EP1716105A1

EP1716105A1 - Method for producing linear pentenenitrile

Info

Publication number: EP1716105A1
Application number: EP05707029A
Authority: EP
Inventors: Tim Jungkamp; Robert Baumann; Michael Bartsch; Gerd Haderlein; Hermann Luyken; Jens Scheidel; Tobias Aechtner; Peter Pfab; Petra Deckert; Peter Bassler; Wolfgang Siegel
Original assignee: BASF SE
Current assignee: BASF SE
Priority date: 2004-01-29
Filing date: 2005-01-27
Publication date: 2006-11-02
Anticipated expiration: 2025-01-27
Also published as: US20080281120A1; ATE507202T1; EP1716105B1; WO2005073174A1; US9493405B2; US20160168082A1; BRPI0507197A; KR20060135785A; DE502005011299D1; KR101152563B1; BRPI0507197B1; US8410299B2; JP4509125B2; US20120178958A1; JP2007519675A; CA2554736A1

Abstract

A process is described for preparing 3-pentenenitrile, characterized by the following process steps: (a) isomerizing a reactant stream which comprises 2-methyl-3-butenenitrile over at least one dissolved or dispersed isomerization catalyst to give a stream 1 which comprises the at least one isomerization catalyst, 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z)-2-methyl-2-butenenitrile, (b) distilling stream 1 to obtain a stream 2 as the top product which comprises 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z)-2-methyl-2-butenenitrile, and a stream 3 as the bottom product which comprises the at least one isomerization catalyst, (c) distilling stream 2 to obtain a stream 4 as the top product which, compared to stream 2, is enriched in (Z)-2-methyl-2-butenenitrile, based on the sum of all pentenenitriles in stream 2, and a stream 5 as the bottom product which, compared to stream 2, is enriched in 3-pentenenitrile and 2-methyl-3-butenenitrile, based on the sum of all pentenenitriles in stream 2, (d) distilling stream 5 to obtain a stream 6 as the bottom product which comprises 3-pentenenitrile and a stream 7 as the top product which comprises 2-methyl-3-butenenitrile.

Description

Process for the preparation of linear pentenenitrile

description

The present invention relates to a process for the preparation of 3-pentenitrile by isomerization of streams containing 2-methyl-3-butenenitrile.

In the production of adiponitrile, an important intermediate in nylon production, 1,3-butadiene is first converted to pentenenitriles with hydrogen cyanide in the presence of nickel (O), which is stabilized with phosphorus ligands. In addition to the main products of hydrocyanation, 3-pentenenitrile and 2-methyl-3-butenenitrile, numerous secondary components are also obtained. Examples include 2-pentenenitriles, 2-methyl-2-butenenitriles, C ₉ nitriles and methylgiutardinitrile. Significant amounts of 2-methyl-3-butenenitrile are formed. Depending on the catalyst used, the molar ratio of 2-methyl-3-butenenitrile to 3-pentenenitrile formed can be up to 2: 1.

In a second hydrocyanation, 3-pentenenitrile is then reacted with hydrogen cyanide to give adiponitrile on the same nickel catalyst with the addition of a Lewis acid. For the second hydrocyanation, it is essential that the 3-pentenenitrile is as free as possible from 2-methyl-3-butenenitrile. Hydrocyanation of 2-methyl-3-butenenitrile would lead to methylgiutardinitrile, which is an undesirable by-product. Accordingly, 3-pentenenitrile and 2-methyl-3-butenenitrile must be separated in an economical process for the production of adiponitrile.

In order to also be able to use 2-methyl-3-butenenitrile for the production of adiponitrile, processes for the isomerization of 2-methyl-3-butenenitrile to linear pentenenitrile, in particular 3-pentenenitrile, have been proposed.

No. 3,676,481 describes the batchwise, batchwise isomerization of 2-methyl-3-butenenitrile in the presence of Ni (0), a phosphite ligand and certain Lewis acids. After the isomerization, the product mixture formed is distilled off from the catalyst system. The disadvantages of this process are the high residence times during the isomerization, the high thermal load on the thermally sensitive catalyst during the isomerization and during the subsequent distillation. The high thermal load on the catalyst leads to an undesirable degradation of the catalyst.

The older, not prepublished German patent application DE 103 11 119.0 from BASF AG describes a process for isomerizing 2-methyl-3-butenenitrile to linear pentenenitrile in the presence of a system containing Ni (0) catalysts and Lewis acids. A mixture containing 2-methyl-3-butenenitrile and linear pentenenitrile is removed from the reaction mixture by distillation during the isomerization. A disadvantage of this method is that the removed sample Duct stream still contains significant amounts of unreacted 2-methyl-3-butenenitrile.

Common to all known processes for the isomerization of 2-methyl-3-butenenitrile is that 2-methyl-3-butenenitrile cannot be completely converted to 3-pentenenitrile because of the thermodynamic equilibrium. Unreacted 2-methyl-3-butenenitrile must be returned to the isomerization step in order to carry out the process economically. In the isomerization of 2-methyl-3-butenenitrile, however, by-product (Z) -2-methyl-2-butenenitrile is obtained, which would level up in the recycle stream if 2-methyl-3-butenenitrile were recycled, since it would be separated off of 3-pentenenitrile passes from the isomerization product stream by distillation because of the very similar vapor pressures together with the 2-methyl-3-butenenitrile.

No. 3,865,865 describes the separation of 2-methyl-2-butenenitrile from a mixture with 2-methyl-3-butenenitrile. The separation is carried out by treating the mixture of the nitriles with an aqueous solution consisting of sulfite and bisulfite ions. This forms the bisulfite adduct of 2-methyl-2-butenenitrile, which passes into the aqueous phase. The resulting organic phase is reduced to 50% of the original 2-methyl-2-butenenitrile content. The process according to US Pat. No. 3,865,865 is cumbersome since a phase separation of an organic phase from an aqueous phase is required. In addition, this separation is difficult to integrate into an overall process for the production of adiponitrile. A further disadvantage of this process is that the organic phase obtained must first be completely freed from water before it can be used further in hydrocyanation reactions using NickeΙ (O) catalysts with phosphorus (III) -containing ligands, since otherwise the phosphorus (III ) -containing ligands are irreversibly hydrolyzed and thus inactivated. Another disadvantage of this process is that the bisulfite adducts obtained can only be split back under drastic conditions and only with a moderate yield in order to continue using the conjugated nitriles, as described in US Pat. No. 3,865,865.

The object of the present invention is therefore to provide a process for the preparation of 3-pentenenitrile by isomerization of 2-methyl-3-butenenitrile, it being possible for the catalyst for the isomerization to be separated off and returned from the reaction mixture in a simple manner, and both the separation of (Z) -2-methyl-2-butenenitrile of 2-methyl-3-butenenitrile as well as the recycling of the 2-methyl-3-butenenitrile depleted in (Z) -2-methyl-2-butenenitrile is made possible. The process should preferably be technically simple and economical to carry out and should be able to be integrated into an overall process for the production of adiponitrile. This object is achieved according to the invention by a process for the preparation of 3-pentenenitrile.

Embodiment I

In one embodiment I, the process is characterized by the following process steps:

(a) isomerization of a starting material stream which contains 2-methyl-3-butenenitrile over at least one dissolved or dispersed isomerization catalyst to a stream 1 which comprises the at least one isomerization catalyst, 2-methyl-3-butenenitrii, 3-pentenenitrile and ( Z) contains -2-methyl-2-butenenitrile,

(b) Distillation of stream 1 to give a stream 2 as overhead product which contains 2-methyl-3-butenenitrii, 3-pentenenitrile and (Z) -2-methyl-2-butenenitrile, and a stream 3 as a bottom product which contains the contains at least one isomerization catalyst,

(c) Distillation of stream 2 to give a stream 4 as top product, which is enriched with respect to stream 2 in (Z) -2-methyl-2-butenenitrile, based on the sum of all pentenenitriles in stream 2, and a stream 5 as a bottom product which is enriched with respect to stream 2 in 3-pentenenitrile and 2-methyl-3-butenenitrile, based on the sum of all pentenenitriles in stream 2,

(d) Distillation of stream 5 to obtain stream 6 as the bottom product which contains 3-pentenenitrile and stream 7 as the top product which contains 2-methyl-3-butenenitrile.

reactant stream

In process step (a) an isomerization of a feed stream which contains 2-methyl-3-butenenitrile takes place on at least one isomerization catalyst.

In a special embodiment of the process according to the invention, the educt stream can be obtained by the following process steps:

(e) Hydrocyanation of 1,3-butadiene on at least one hydrocyanation catalyst using hydrogen cyanide to give a stream 8 which comprises the at least one hydrocyanation catalyst, 3-pentenenitrile, 2-methyl-3-butenenitrile, 1,3-butadiene and residues of hydrogen cyanide contains (f) Single or multiple distillation of stream 8 to obtain stream 9 which contains 1,3-butadiene, stream 10 which contains the at least one hydrocyanation catalyst and stream 11 which comprises 3-pentenenitrile and 2- Contains methyl-3-butenenitrile,

(g) Distillation of stream 11 to give stream 12 as the bottoms product containing 3-pentenenitrile and stream 13 as the overhead product containing 2-methyl-3-butenenitrile.

In process step (e), for the preparation of the educt stream, a hydrocyanation of 1,3-butadiene is first carried out over at least one hydrocyanation catalyst with hydrogen cyanide, while obtaining a stream 8 which comprises the at least one hydrocyanation catalyst, 3-pentenenitrile, 2-methyl-3-butenenitrile and contains unreacted 1,3-butadiene.

A homogeneous nickel (O) catalyst which is stabilized with phosphorus ligands is preferably used as the hydrocyanation catalyst.

The phosphorus-containing ligands of the nickel (0) complexes and the free phosphorus-containing ligands are preferably selected from mono- or bidentate phosphines, phosphites, phosphinites and phosphonites.

These phosphorus-containing ligands preferably have the formula I: P (X ¹ R ¹ ) (X ² R ² ) (X ³ R ³ ) (I)

For the purposes of the present invention, compound I is understood to mean a single compound or a mixture of different compounds of the aforementioned formula.

According to the invention, X ¹ , X ² , X ^{3 are} independently oxygen or a single bond. If all of the groups X ¹ , X ² and X ^{3 are} individual bonds, compound I is a phosphine of the formula P (R ¹ R ² R ³ ) with the meanings given for R ¹ , R ² and R ³ in this description ,

If two of the groups X ¹ , X ² and X ^{3 are} individual bonds and one is oxygen, compound I is a phosphinite of the formula P (OR ¹ ) (R ² ) (R ³ ) or P (R ¹ ) (OR ² ) (R ³ ) or P (R ¹ ) (R ² ) (OR ³ ) with the meanings given below for R ¹ , R ² and R ³ .

If one of the groups X ¹ , X ² and X ^{3 stands} for a single bond and two for oxygen, compound I represents a phosphonite of the formula P (OR ¹ ) (OR ² ) (R ³ ) or P (R ¹ ) (OR ² ) (OR ³ ) or P (OR ¹ ) (R ² ) (OR ³ ) with the meanings given for R ² and R ³ in this description.

In a preferred embodiment, all of the groups X ¹ , X ² and X ³ should stand for oxygen, so that compound I is advantageously a phosphite of the formula

P represents (OR ¹ ) (OR ² ) (OR ³ ) with the meanings given below for R ¹ , R ² and R ³ .

According to the invention, R ¹ , R ² , R ³ independently of one another represent identical or different organic radicals. R ¹ , R ² and R ³ are, independently of one another, alkyl radicals, preferably having 1 to 10 carbon atoms, such as methyl, ethyl, n-propyl, i-propyl, n-butyl, i-butyl, s-butyl, t-butyl, Aryl groups, such as phenyl, o-tolyl, m-tolyl, p-tolyl, 1-naphthyl, 2-naphthyl, or hydrocarbyl, preferably having 1 to 20 carbon atoms, such as I. L'-biphenol, 1,1'- Binaphthol into consideration. The groups R \ R ² and R ³ can be connected to one another directly, that is to say not only via the central phosphorus atom. The groups R ¹ , R ² and R ³ are preferably not directly connected to one another.

In a preferred embodiment, groups R ¹ , R ² and R ³ are selected from the group consisting of phenyl, o-tolyl, m-tolyl and p-tolyl. In a particularly preferred embodiment, a maximum of two of the groups R ¹ , R ² and R ^{3 should be} phenyl groups.

In another preferred embodiment, a maximum of two of the groups R ¹ , R ² and R ^{3 should be} o-tolyl groups.

Particularly preferred compounds I are those of the formula I a

(o-tolyl-O-) _w (m-tolyl-O-) _x (p-tolyl-O-) _y (phenyl-O-) _z P (I a)

are used, where w, x, y and z represent a natural number, and the following conditions apply: w + x + y + z = 3 and w, z <2.

Such compounds I a are, for example, (p-tolyl-O -) (phenyl-O-) ₂ P, (m-tolyl-O -) (phenyl-O-) ₂ P, (o-tolyl-O-) (phenyl -O-) ₂ P, (p-tolyl-O-) ₂ (phenyl-O-) P, (m-tolyl-O-) ₂ (phenyl-O-) P, (o-tolyl-O-) ₂ (Phenyl-O-) P, (m-tolyl-O -) (p-tolyl-O) (phenyl-O-) P, (o-tolyl-O -) (p-tolyl-O -) (phenyl- O-) P, (o-tolyl-O -) (m-tolyl-O -) (phenyl-O-) P, (p-tolyl-O-) ₃ P, (m-tolyl-O -) (p -Tolyi-O-) ₂ P, (o-Tolyi-O -) (p-tolyl-O-) 2P, (m-tolyl-O-) ₂ (p-tolyl-O-) P, (o-tolyl - O-) ₂ (p-tolyl-O-) P, (o-TolyI-O -) (m-tolyl-O -) (p-tolyl-O) P, (m-tolyl-O-) ₃ P , (o-tolyl-O -) (m-tolyl-O-) ₂ P (o-tolyl-O-) ₂ (m-tolyl-O-) P, or mixtures of such compounds. Mixtures containing (m-tolyl-O-) ₃ P, (m-tolyl-O-) ₂ (p-tolyl-O-) P, (m-tolyl-O -) (p-tolyl-O-) P and (p-Tolyl-O-) ₃ P can be obtained, for example, by reacting a mixture containing m-cresol and p-cresol, in particular in a molar ratio of 2: 1, as is obtained in the working up of petroleum by distillation, with a phosphorus trihalide, such as phosphorus trichloride. receive.

In another, likewise preferred embodiment, the phosphites of the formula Ib described in more detail in DE-A 199 53058 are suitable as phosphorus-containing ligands:

P (OR ¹ ) _x (OR ² ) _y (OR ³ ) _z (OR ⁴ ) _p (I b)

With

R ¹ : aromatic radical with a CrC ₁₈ -alkyl substituent in the o-position to the oxygen atom which connects the phosphorus atom to the aromatic system, or with an aromatic substituent in the o-position to the oxygen atom which connects the phosphorus atom to the aromatic system, or with an aromatic system fused in the o-position to the oxygen atom, which connects the phosphorus atom with the aromatic system,

R ² : aromatic radical with a C Ci ₈ alkyl substituent in the m-position to the oxygen atom that connects the phosphorus atom to the aromatic system, or with an aromatic substituent in the m-position to the oxygen atom that connects the phosphorus atom with the aromatic system System, or with an aromatic system fused to the oxygen atom that connects the phosphorus atom to the aromatic system, the aromatic radical in the o-position to the oxygen atom that connects the phosphorus atom to the aromatic system, carries a hydrogen atom,

R ³ : aromatic radical with a CC ₁₈ -alkyl substituent in the p-position to the oxygen atom that connects the phosphorus atom to the aromatic system, or with an aromatic substituent in the p-position to the oxygen atom that connects the phosphorus atom to the aromatic system, the aromatic radical in the o-position to the oxygen atom that connects the phosphorus atom to the aromatic system carries a hydrogen atom,

R ⁴ : aromatic radical which, in the o-, m- and p-position to the oxygen atom which connects the phosphorus atom to the aromatic system, bears other substituents than those defined for R ¹ , R ² and R ³ , the aromatic radical in o-position to the oxygen atom, which is the phosphorus atom with the aromatic system connects, carries a hydrogen atom,

x: 1 or 2,

y, z, p: independently of one another 0, 1 or 2 with the proviso that x + y + z + p = 3.

Preferred phosphites of the formula Ib can be found in DE-A 199 53 058. The radical R ¹ advantageously includes o-tolyl, o-ethyl-phenyl, on-propyl-phenyl, o-isopropyl-phenyl, on-butyl-phenyl, o-sec-butyl-phenyl, o- tert-Butyl-phenyl, (o-phenyl) -phenyl or 1-naphthyl groups into consideration.

The radical R ² is m-tolyl, m-ethyl-phenyl, mn-propyl-phenyl, m-isopropyl-phenyl, m-butyl-phenyl, m-sec-butyl-phenyl, m-tert -Butyl-phenyl, (m-phenyl) -phenyl or 2-naphthyl groups preferred.

The radical R ³ is advantageously p-tolyl, p-ethyl-phenyl, pn-propyl-phenyl, p-isopropyl-phenyl, pn-butyl-phenyl, p-sec-butyl-phenyl, p- tert-Butyl-phenyl or (p-phenyl) phenyl groups into consideration.

R ⁴ is preferably phenyl. P is preferably zero. The following options result for the indices x, y, z and p in connection I b:

Preferred phosphites of the formula Ib are those in which p is zero and R ¹ , R ² and R ³ are selected independently of one another from o-isopropylphenyl, m-tolyl and p-tolyl, and R ^{4 is} phenyl.

Particularly preferred phosphites of the formula Ib are those in which R ^{1 is} the o-isopropylphenyl radical, R ^{2 is} the m-tolyl radical and R ^{3 is} the p-tolyl radical with the indices mentioned in the table above; also those in which R ^{1 is} the o-tolyl radical, R ^{2 is} the m-tolyl radical and R ^{3 is} the p-tolyl radical with the indices specified in the table; furthermore those in which R ^{1 is} the 1-naphthyl radical, R ^{2 is} the m-tolyl radical and R ^{3 is} the p- Tolyl residue is with the indices mentioned in the table; also those in which R ^{1 is} the o-tolyl radical, R ^{2 is} the 2-naphthyl radical and R ^{3 is} the p-tolyl radical with the indices specified in the table; and finally those in which R ^{1 is} the o-isopropylphenyl radical, R ^{2 is} the 2-naphthyl radical and R ^{3 is} the p-tolyl radical with the indices given in the table; as well as mixtures of these phosphites.

Phosphites of formula I b can be obtained by

a) reacting a phosphorus trihalide with an alcohol selected from the group consisting of R ¹ OH, R ² OH, R ³ OH and R ⁴ OH or mixtures thereof to obtain a dihalophosphoric acid monoester,

b) the said dihalophosphoric acid monoester is reacted with an alcohol selected from the group consisting of R ¹ OH, R ² OH, R ³ OH and R ⁴ OH or their mixtures to obtain a monohalophosphoric acid diester and

c) the said monohalophosphoric diester is reacted with an alcohol selected from the group consisting of R ¹ OH, R ² OH, R ³ OH and R OH or mixtures thereof to give a phosphite of the formula I b.

The implementation can be carried out in three separate steps. Two of the three steps can also be combined, i.e. a) with b) or b) with c). Alternatively, all of steps a), b) and c) can be combined with one another.

Suitable parameters and amounts of the alcohols selected from the group consisting of R ¹ OH, R ² OH, R ³ OH and R ⁴ OH or their mixtures can easily be determined by a few simple preliminary tests.

Suitable phosphorus trihalides are in principle all phosphorus trihalides, preferably those in which Cl, Br, I, in particular Cl, is used as the halide, and mixtures thereof. Mixtures of different identical or different halogen-substituted phosphines can also be used as the phosphorus trihalide. PCI ₃ is particularly preferred. Further details on the reaction conditions in the preparation of the phosphites Ib and on the workup can be found in DE-A 199 53 058.

The phosphites Ib can also be used as a ligand in the form of a mixture of different phosphites Ib. Such a mixture can occur, for example, in the production of the phosphites Ib. However, it is preferred that the phosphorus-containing ligand is multidentate, in particular bidentate. The ligand used therefore preferably has the formula II

on what mean

X ¹¹ , X ¹² , X ¹³ , X ²¹ , X ²² , X ²³ independently of one another oxygen or single bond

R ¹¹ , R ¹² independently of one another the same or different, individual or bridged organic radicals

R ²¹ , R ²² independently of one another the same or different, single or bridged organic radicals, bridging group

For the purposes of the present invention, compound II is understood to mean a single compound or a mixture of different compounds of the abovementioned formula.

In a preferred embodiment, X ¹¹ , X ¹² , X ¹³ , X ²¹ , X ²² , X ²³ can represent oxygen. In such a case, the bridging group Y is linked to phosphite groups.

In another preferred embodiment, X ¹¹ and X ¹² oxygen and X ^{13 can be} a single bond or X ¹¹ and X ¹³ oxygen and X ¹² can be a single bond, so that the phosphorus atom surrounded by X ¹¹ , X ¹² and X ^{13 is the} central atom of a phosphonite. In such a case, X ²¹ , X ²² and X ²³ oxygen or X ²¹ and X ²² oxygen and X ²³ a single bond or X ²¹ and X ²³ oxygen and X ²² a single bond or X ²³ oxygen and X ²¹ and X ²² a single bond or X ²¹ oxygen and X ²² and X ^{23 represent} a single bond or X ²¹ , X ²² and X ^{23 represent} a single bond, so that the phosphorus atom surrounded by X ²¹ , X ²² and X ²³ preferably represents a phosphite, phosphonite, phosphinite or phosphine of a phosphonite.

In another preferred embodiment, X ¹³ oxygen and X ¹¹ and X ^{12 may be} a single bond or X ¹¹ oxygen and X ¹² and X ¹³ may be a single bond, so that the phosphorus atom surrounded by X ¹¹ , X ¹² and X ^{13 is a} central atom Is phosphonite. In such a case, X ²¹ to X ²² and X ²³ is oxygen or X ²³ oxygen and X ²¹ and X ²² is a single bond, or X ²¹ is oxygen and X ²² and X ²³ is a single bond or X ^21, X ²² and X ²³ represent a single bond, so that the phosphorus atom surrounded by X ²¹ , X ²² and X ^{23 can be the} central atom of a phosphite, phosphinite or phosphine, preferably a phosphinite.

In another preferred embodiment, X ¹¹ , X ¹² and X ^{13 can represent} a single bond, so that the phosphorus atom surrounded by X ¹¹ , X ¹² and X ^{13 is the} central atom of a phosphine. In such a case, X ²¹ , X ²² and X ²³ oxygen or X ²¹ , X ²² and X ^{23 represent} a single bond, so that the phosphorus atom surrounded by X ²¹ , X ²² and X ^{23 is the} central atom of a phosphite or phosphine, preferably a phosphine , can be.

Preferred bridging groups Y are substituted, for example with CC-alkyl, halogen, such as fluorine, chlorine, bromine, halogenated alkyl, such as trifluoromethyl, aryl, such as phenyl, or unsubstituted aryl groups, preferably those having 6 to 20 carbon atoms in the aromatic system, in particular pyrocatechol, bis (phenol) or bis (naphthol).

The radicals R ¹¹ and R ¹² can independently represent the same or different organic radicals. R ¹¹ and R ¹² are advantageously aryl radicals, preferably those having 6 to 10 carbon atoms, which can be unsubstituted or mono- or polysubstituted, in particular by CrC- _4- alkyl, halogen, such as fluorine, chlorine, bromine or halogenated Alkyl, such as trifluoromethyl, aryl, such as phenyl, or unsubstituted aryl groups.

The radicals R ²¹ and R ²² can independently represent the same or different organic radicals. Advantageously suitable as radicals R ²¹ and R ^{22 are} aryl radicals, preferably those having 6 to 10 carbon atoms, which can be unsubstituted or mono- or polysubstituted, in particular by C 1 -C ₄ -alkyl, halogen, such as fluorine, chlorine, bromine, halogenated alkyl such as trifluoromethyl, aryl such as phenyl or unsubstituted aryl groups.

The radicals R ¹¹ and R ¹² can be individually or bridged. The radicals R ²¹ and R ²² can also be individual or bridged. The radicals R ¹¹ , R ¹² , R ²¹ and R ²² can all be individually, two bridged and two individually or all four bridged in the manner described.

In a particularly preferred embodiment, the compounds of the formula I, II, III, IV and V mentioned in US Pat. No. 5,723,641 are suitable. In a particularly preferred embodiment, the compounds of the formulas I, II, III, IV, V, VI and VII mentioned in US Pat. No. 5,512,696, in particular those in Examples 1 to 31 used connections, into consideration. In a particularly preferred embodiment, the compounds of the formula I, II, III, IV, V, VI, VII, VIII, IX, X, XI, XII, XII, XIV and XV mentioned in US Pat. No. 5,821,378, in particular those in the examples 1 to 73 compounds used.

In a particularly preferred embodiment, the compounds of the formula I, II, III, IV, V and VI mentioned in US Pat. No. 5,512,695, in particular the compounds used there in Examples 1 to 6, come into consideration. In a particularly preferred embodiment, the compounds of the formula I, II, IM, IV, V, VI, VII, VIII, IX, X, XI, XII, XIII and XIV mentioned in US Pat. No. 5,981,772, in particular those in Examples 1 to 4 66 connections used.

In a particularly preferred embodiment, the compounds mentioned in US Pat. No. 6,127,567 and the compounds used there in Examples 1 to 29 are suitable. In a particularly preferred embodiment, the compounds of the formula I, II, III, IV, V, VI, VII, VIII, IX and X mentioned in US Pat. No. 6,020,516, in particular the compounds used there in Examples 1 to 33, come into consideration. In a particularly preferred embodiment, the compounds mentioned in US Pat. No. 5,959,135 and the compounds used there in Examples 1 to 13 come into consideration.

In a particularly preferred embodiment, the compounds of the formula I, II and III mentioned in US Pat. No. 5,847,191 are suitable. In a particularly preferred embodiment, the compounds mentioned in US Pat. No. 5,523,453, in particular those in formulas 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18, 19, 20 and 21 connections shown. In a particularly preferred embodiment, the compounds mentioned in WO 01/14392, preferably those there in the formulas V, VI, VII, VIII, IX, X, XI, XII, XIII, XIV, XV, XVI, XVII, XXI, XXII, XXIII compounds shown.

In a particularly preferred embodiment, the compounds mentioned in WO 98/27054 are suitable. In a particularly preferred embodiment, the compounds mentioned in WO 99/13983 are suitable. In a particularly preferred embodiment, the compounds mentioned in WO 99/64155 come into consideration.

In a particularly preferred embodiment, the compounds mentioned in German patent application DE 100 380 37 come into consideration. In a particularly preferred embodiment, the compounds mentioned in German patent application DE 100460 25 come into consideration. In a particularly preferred embodiment, the compounds mentioned in German patent application DE 101 502 85 come into consideration. In a particularly preferred embodiment, the compounds mentioned in German patent application DE 101 502 86 come into consideration. In a particularly preferred embodiment, the compounds mentioned in German patent application DE 102071 65 come into consideration. In a further particularly preferred embodiment of the present invention, the phosphorus-containing chelate ligands mentioned in US 2003/0100442 A1 come into consideration.

In a further particularly preferred embodiment of the present invention, the phosphorus-containing chelate ligands mentioned in the unpublished German patent application file number DE 103 50 999.2 dated October 30, 2003 come into consideration.

The compounds I, I a, I b and II described and their preparation are known per se. Mixtures containing at least two of the compounds I, I a, I b and II can also be used as the phosphorus-containing ligand.

In a particularly preferred embodiment of the process according to the invention, the phosphorus-containing ligand of the nickel (0) complex and / or the free phosphorus-containing ligand is selected from tritolylphosphite, bidentate phosphorus-containing chelate ligands, and the phosphites of the formula Ib

P (OR ¹ ) _x (OR ² ) _y (OR ³ ) _z (OR ⁴ ) _p (I b)

wherein R ¹ , R ² and R ^{3 are} independently selected from o-isopropyl-phenyl, m-tolyl and p-tolyl, R ^{4 is} phenyl; x is 1 or 2 and y, z, p are independently 0, 1 or 2 with the proviso that x + y + z + p = 3; and their mixtures.

Process step (e) can be carried out in any suitable apparatus known to the person skilled in the art. Conventional apparatuses are therefore suitable for the reaction, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 20, John Wiley & Sons, New York, 1996, pages 1040 to 1055, such as stirred tank reactors, loop reactors, gas circulation reactors, bubble column reactors or tubular reactors, each optionally with devices for removing heat of reaction. The reaction can be carried out in several, such as two or three, apparatus.

In a preferred embodiment of the process according to the invention, reactors with backmixing characteristics or cascades of reactors with backmixing characteristics have proven to be advantageous. Cascades from reactors with backmixing characteristics have proven to be particularly advantageous with regard to the metering of hydrogen cyanide in cross-flow mode.

The hydrocyanation can be carried out in the presence or absence of a solvent. If a solvent is used, the solvent should be liquid at the given reaction temperature and the given reaction pressure and inert to the unsaturated compounds and the at least one catalyst. In general, hydrocarbons, for example benzene or xylene, or nitriles, for example acetonitrile or benzonitrile, are used as solvents. However, a ligand is preferably used as the solvent.

The reaction can be carried out in batch mode, continuously or in semi-batch mode.

The hydrocyanation reaction can be carried out by loading all reactants into the device. However, it is preferred if the device is filled with the catalyst, the unsaturated organic compound and, if appropriate, the solvent. The gaseous hydrogen cyanide preferably hovers over the surface of the reaction mixture or is passed through the reaction mixture. Another procedure for equipping the device is to fill the device with the catalyst, hydrogen cyanide and, if appropriate, the solvent and to slowly feed the unsaturated compound into the reaction mixture. Alternatively, it is also possible for the reactants to be introduced into the reactor and for the reaction mixture to be brought to the reaction temperature at which the hydrogen cyanide is added to the mixture in liquid form. In addition, the hydrogen cyanide can also be added before heating to the reaction temperature. The reaction is carried out under conventional hydrocyanation conditions for temperature, atmosphere, reaction time, etc.

The hydrocyanation is preferably carried out continuously in one or more stirred process steps. If a plurality of method steps are used, it is preferred that the method steps are connected in series. The product is transferred directly from one process step to the next process step. The hydrogen cyanide can be fed directly into the first process step or between the individual process steps.

If the process according to the invention is carried out in semibatch operation, it is preferred that the catalyst components and 1,3-butadiene are placed in the reactor while hydrogen cyanide is metered into the reaction mixture over the reaction time. The reaction is preferably carried out at absolute pressures of 0.1 to 500 MPa, particularly preferably 0.5 to 50 MPa, in particular 1 to 5 MPa. The reaction is preferably carried out at temperatures from 273 to 473 K, particularly preferably 313 to 423 K, in particular at 333 to 393 K. Average residence times of the liquid reactor phase in the range from 0.001 to 100 hours, preferably 0.05 to 20 hours, particularly preferably 0.1 to 5 hours, in each case per reactor, have proven advantageous.

In one embodiment, the reaction can be carried out in the liquid phase in the presence of a gas phase and, if appropriate, a solid suspended phase. The starting materials hydrogen cyanide and 1,3-butadiene can each be metered in in liquid or gaseous form.

In a further embodiment, the reaction can be carried out in the liquid phase, the pressure in the reactor being such that all the starting materials, such as 1,3-butadiene, hydrogen cyanide and the at least one catalyst, are metered in liquid and are present in the liquid phase in the reaction mixture. A solid suspended phase can be present in the reaction mixture, which can also be metered in together with the at least one catalyst, for example consisting of degradation products of the catalyst system containing, inter alia, nickel (II) compounds.

In process step (e), a stream 8 which contains 3-pentenenitrile, 2-methyl-3-butenenitrile, at least one catalyst and unreacted 1,3-butadiene is obtained.

Stream 8, which contains 3-pentenenitrile, 2-methyl-3-butenenitrile, the at least one catalyst and unreacted 1,3-butadiene, is then transferred to a distillation apparatus in process step (f). In this distillation device, a single or multiple distillation of stream 8 takes place to obtain stream 9 which contains 1,3-butadiene, stream 10 which contains the at least one hydrocyanation catalyst and stream 11 which comprises 3-pentenenitrile and 2-methyl Contains -3-butenenitrile.

Process step (f) can be distilled in two stages, as described in DE-A-102 004 004720, process steps (b) and (c). Process step (f) can also be distilled according to DE-A-102 004 004729, process steps (b) and (c).

The distillation (s) of process step (f) can be carried out in any suitable apparatus known to the person skilled in the art. Equipment suitable for distillation, as described, for example, in: Kirk-Othmer, Encyciopedia of Chemical

Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pp. 334-348. are written, such as sieve tray columns, bubble tray trays, packing columns, packed columns, which can also be operated as dividing wall columns. These distillation units are each equipped with suitable devices for evaporation, such as falling-film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, as well as devices for condensing the vapor stream. The individual distillations can be carried out in several, such as two or three apparatuses, advantageously in a single apparatus.

The distillation (s) can also be carried out in one stage in the sense of partial evaporation of the feed stream.

The pressure in process step (f) is preferably 0.001 to 10 bar, particularly preferably 0.010 to 1 bar, in particular 0.02 to 0.5 bar. The distillation (s) is / are carried out so that the temperature (s) towards the bottom of the Destillationsvor- (s) preferably 30 to 200 ° C, particularly preferably 50 to 150 ^C C, in particular 60 to 120 ° C, is / be. The distillation (s) is / are carried out in such a way that the condensation temperatures at the top of the distillation apparatus are preferably -50 to 150 ° C., particularly preferably -15 to 60 ° C., in particular 5 to 45 ° C. In a particularly preferred embodiment of the process according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom of the distillation device (s).

Stream 11 is then subjected to distillation in a further process step (g). This distillation can be carried out in any suitable apparatus known to the person skilled in the art. Equipment suitable for distillation, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, such as sieve plate columns, Bell-bottom columns, packed columns, packed columns, which can also be operated as dividing wall columns. These distillation units are each equipped with suitable devices for evaporation, such as falling-film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, as well as devices for condensing the vapor stream. The distillation can advantageously be carried out in several, such as two or three, apparatuses in a single apparatus. The distillation can also be carried out in one stage in the sense of partial evaporation of the feed stream.

The pressure in process step (g) is preferably 0.001 to 100 bar, particularly preferably 0.01 to 20 bar, in particular 0.05 to 2 bar. The distillation is carried out so that the temperature in the bottom of the distillation device is preferably 30 to 250 ° C., particularly preferably 50 to 200 ° C., in particular 60 to 180 ° C. The distillation is carried out in such a way that the condensation temperature at the top of the distillation device is preferably from -50 to 250 ° C., particularly preferably from 0 to 180 ° C., in particular from 15 to 160 ° C. In a particularly preferred embodiment of the process according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom of the distillation device.

In process step (g), a stream 12 is obtained as the bottom product, which contains 1,3-pentenenitrile, and stream 13 as the top product, which contains 2-methyl-3-butenenitrile. Stream 13 is preferably used as a feed stream in the process according to the invention for the production of 3-pentenenitrile.

In further preferred embodiments of the process according to the invention, stream 8 obtained in process step (e) is transferred directly to process step (g). In this process step (g), a stream is then obtained via the bottom which essentially comprises 3-pentenenitrile and the at least one hydrocyanation catalyst. In addition, a stream is obtained overhead, which essentially contains 2-methyl-3-butenenitrile and 1,3-butadiene. This stream, which is rich in 2-methyl-3-butenenitrile and 1,3-butadiene, can also be used as a feed stream in the process according to the invention for the production of 3-pentenenitrile. If this feed stream is used in the process according to the invention, the content of 2-methyl-3-butenenitrile in this stream is preferably 10 to 90% by weight, particularly preferably 20 to 85% by weight, in particular 30 to 80% by weight. -%, each based on the current.

Alternatively, it is also possible to reduce the stream 8 obtained in process step (e) only to 1,3-butadiene in process step (f). A stream 11a is then obtained via the bottom of process step (f), which essentially contains 3-pentenenitrile, 2-methyl-3-butenenitrile and the at least one hydrocyanation catalyst. This stream 11a is then worked up further in process step (g) with the separation of 3-pentenenitrile and the at least one hydrocyanation catalyst on the one hand and 2-methyl-3-butenenitrile on the other hand. Stream 13a from process step (g) at the top of the distillation essentially contains 2-methyl-3-butenenitrile. This stream 13a can also be used as a feed stream in the process according to the invention for the production of 3-pentenenitrii.

In a further embodiment, stream 8 from process step (e) in process step (f) is only depleted of 1,3-butadiene and transferred to process step (g), where a stream 12 with 3-pentenenitrile and the hydrocyanation catalyst is in the bottom is obtained. In a further embodiment of the present invention, a feed stream is used which originates from a hydrocyanation of process step (e) and a subsequent workup in process step (f), wherein in process step (f) only 1,3-butadiene is optionally depleted , The resulting stream 11b is then transferred to process step (a) of the process according to the invention. The hydrocyanation catalyst contained in this stream 11b is then preferably used as the at least one isomerization catalyst in process step (a) of the process according to the invention. A suitable Lewis acid can also be added, as described, for example, in DE-A-102004 004696.

In a further embodiment of the present invention, it is possible for the feed stream used in process step (a) according to the invention to correspond to stream 11 of process step (f), so that stream 11 is not separated in process step (g).

In a further embodiment of the process according to the invention, stream 8, which originates from process step (e), is used as the educt stream. In this case, process steps (f) and (g) in the production of the educt stream for the process according to the invention are therefore omitted.

Process step (a)

In process step (a), an isomerization of the educt stream which contains 2-methyl-3-butenenitrile takes place on at least one isomerization catalyst. A stream 1 is obtained which contains the isomerization catalyst, unreacted 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z) -2-methyl-2-butenenitrile.

According to the invention, the isomerization is carried out in the presence of a system comprising a) nickel (O), b) a compound containing triple-bonded phosphorus and complexing as a ligand, and optionally c) a Lewis acid.

Catalyst systems containing nickel (O) can be prepared by processes known per se.

The same phosphorus-containing ligands as for the hydrocyanation catalyst used in process step (e) can be used as ligands for the isomerization catalyst. gate can be used. Thus, the hydrocyanation catalyst can be identical to the isomerization catalyst. The selection of the ligands for the reactions in process steps (a) and (e) does not necessarily have to be the same.

The system may also contain a Lewis acid.

For the purposes of the present invention, a Lewis acid is understood to mean a single Lewis acid or a mixture of several, such as two, three or four Lewis acids.

Suitable Lewis acids are inorganic or organic metal compounds in which the cation is selected from the group consisting of scandium, titanium, vanadium, chromium, manganese, iron, cobalt, copper, zinc, boron, aluminum , Yttrium, zirconium, niobium, molybdenum, cadmium, rhenium and tin. Examples are ZnBr ₂ , Znl ₂ , ZnCI ₂ , ZnSO ₄ , CuCI ₂ , CuCI, Cu (O ₃ SCF ₃ ) 2, CoCI ₂ , Col ₂ , Fel ₂ , FeCI ₃ , FeCI ₂ , FeCI ₂ (THF) _2l TiCI ₄ (THF) _2l TiCI ₄ , TiCI ₃ , CITi (Oi-Propyl) ₃ , MnCI ₂ , ScCI ₃ , AICI ₃ , (C ₈ H ₁₇ ) AICI ₂ , (C ₈ H ₁₇ ) ₂ AICI, (iC ₄ H ₉ ) ₂ AICI, (C ₆ H ₅ ) ₂ AICI, (C ₆ H ₅ ) AICI ₂ , ReCI ₅₎ ZrCI ₄ , NbCI ₅ , VCI ₃ , CrCl ₂ , M0CI ₅ , YCI ₃ , CdCI ₂ , LaCI ₃ , Er (O ₃ SCF ₃₎ ₃₎ Yb (O ₂ CCF ₃₎ _3l SMCI _3, B (C ₆ H ₅₎ _3, TaCI _5, such as in US 6,127,567, US 6,171,996 and US 6,380,421 described ben. Also suitable are metal salts, such as ZnCl ₂ , Col ₂ and SnCl _2, and organometallic compounds, such as RAICI _2> R ₂ AICI, RSnO ₃ SCF ₃ and R ₃ B, where R is an alkyl or aryl group, such as described for example in US 3,496,217, US 3,496,218 and US 4,774,353. According to US Pat. No. 3,773,809, a metal in cationic form, selected from the group consisting of zinc, cadmium, beryllium, aluminum, gallium, indium, thallium, titanium, zirconium, hafnium, erbium, germanium, tin, vanadium, niobium, can also be used as a promoter. Scandium, chromium, molybdenum, tungsten, manganese, rhenium, palladium, thorium, iron and cobalt, preferably zinc, cadmium, titanium, tin, chromium, iron and cobalt, can be used, and the anionic part of the compound can be selected from the group , consisting of halides, such as fluoride, chloride, bromide and iodide, anions of lower fatty acids with from 2 to 7 carbon atoms, HPO ₃ ^{2 "} , H ₃ PO ^2" , CF ₃ COO ^' , C ₇ H ₁₅ OSO ₂ ^" or SO ₄ ^{2 "} . Further suitable promoters from US Pat. No. 3,773,809 are borohydrides, organoborohydrides and boric acid esters of the formula R ₃ B and B (OR) ₃ , where R is selected from the group consisting of hydrogen, aryl radicals having between 6 and 18 carbon atoms Alkyl groups with 1 to 7 carbon atoms substituted aryl radicals and aryl radicals substituted with cyano-substituted alkyl groups with 1 to 7 carbon atoms, advantageously triphenylboron. Furthermore, as described in US 4,874,884, synergistically effective combinations of Lewis acids can be used to increase the activity of the catalyst system. Suitable promoters can be selected, for example, from the group consisting of CdCl ₂ , FeCI ₂ , ZnCI ₂ , B (C ₆ H ₅ ) ₃ and (C ₆ H ₅ ) ₃ SnX, with X = CF ₃ SO ₃ , CH ₃ C ₆ H ₄ SO ₃ or (C ₆ H ₅ ) ₃ BCN can be selected, a range of preferably about 1:16 to about 50: 1 being mentioned for the ratio of promoter to nickel.

For the purposes of the present invention, the term Lewis acid also includes the promoters mentioned in US 3,496,217, US 3,496,218, US 4,774,353, US 4,874,884, US 6,127,567, US 6,171,996 and US 6,380,421.

Lewis acids which are particularly preferred are those metal salts, particularly preferably metal halides, such as fluorides, chlorides, bromides, iodides, in particular chlorides, of which zinc chloride, iron-CIO chloride and iron (III) chloride in turn are particularly preferred.

The isomerization can be carried out in the presence of a liquid diluent,

- For example, a hydrocarbon such as hexane, heptane, octane, cyclohexane, methylcyclohexane, benzene, decahydronaphthalene

- for example an ether, such as diethyl ether, tetrahydrofuran, dioxane, glycol dimethyl ether, anisole,

- For example, an ester such as ethyl acetate, methyl benzoate, or

- For example, a nitrile, such as acetonitrile, benzonitrile, or - Mixtures of such diluents are carried out.

In a particularly preferred embodiment, isomerization in the absence of such a liquid diluent can be considered.

It has also proven to be advantageous if the isomerization in process step (a) is carried out in a non-oxidizing atmosphere, such as, for example, under a protective gas atmosphere made of nitrogen or a noble gas, such as argon.

Process step (a) can be carried out in any suitable apparatus known to the person skilled in the art. Conventional apparatuses are suitable for the reaction, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 20, John Wiley & Sons, New York, 1996, pages 1040 to 1055, such as stirred tank reactors, loop reactors, gas circulation reactors, bubble column reactors or tubular reactors. The reaction can be carried out in several, such as two or three, apparatus.

In a preferred embodiment of the process according to the invention, the isomerization is carried out in a compartmentalized tubular reactor.

In a further preferred embodiment of the process according to the invention, the isomerization is carried out in at least two reactors connected in series. leads, wherein the first reactor essentially has a stirred tank characteristic and the second reactor is designed such that it essentially has a tube characteristic.

In a particularly preferred embodiment of the process according to the invention, the isomerization is carried out in a reactor, the reactor having the characteristic of a stirred tank cascade which corresponds to 2 to 20 stirred tanks, in particular 3 to 10 stirred tanks.

In one embodiment of the process according to the invention, the reaction can be carried out in a distillation apparatus, the isomerization reaction taking place at least in the bottom region of the distillation apparatus. Any distillation apparatus known to the person skilled in the art, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, is suitable Sieve tray columns, bubble tray trays, packing columns, packed columns, which can also be operated as a dividing wall column. These distillation units are each equipped with suitable devices for evaporation, such as falling-film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, as well as devices for condensing the vapor stream. The distillation with the reaction taking place simultaneously can advantageously be carried out in several, such as two or three, apparatuses in a single apparatus. The distillation can also be carried out in one stage in the sense of partial evaporation of the feed stream.

Process step (a) of the process according to the invention is preferably carried out at an absolute pressure of 0.1 mbar to 100 bar, particularly preferably 1 mbar to 16 bar, in particular 10 mbar to 6 bar. The temperature in process step (a) is preferably 25 to 250 ° C., particularly preferably 30 to 180 ° C., in particular 40 to 140 ° C.

The composition of the withdrawn stream in terms of the molar ratio of 2-methyl-3-butenenitrile to linear pentenenitrile and thus the degree of conversion of 2-methyl-3-butenenitrile used can be determined in a technically simple manner depending on the composition of the stream supplied by the temperature, the catalyst concentration, the residence time and the design of the reactor are adjusted. In a preferred embodiment of the process according to the invention, the degree of conversion is adjusted to values in the range of 10 to 99%, particularly preferably 30 to 95%, in particular 60 to 90%, using these measures.

Process step (b) In process step (b), stream 1 obtained in process step (a) is distilled. The top product obtained is a stream 2 which contains 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z) -2-methyl-2-butenenitrile. In addition, in process step (b) a stream 3 is obtained as the bottom product, which contains the at least one isomerization catalyst.

Process step (b) of the process according to the invention can be carried out in any suitable distillation apparatus known to the person skilled in the art. Equipment suitable for distillation, as described for example in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, as Sieve tray columns, bubble tray trays, packed columns, packed columns, which can also be operated as dividing wall columns. These distillation units are each equipped with suitable devices for evaporation, such as falling-film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, as well as devices for condensing the vapor stream. The distillation can advantageously be carried out in several, such as two or three, apparatuses in a single apparatus. The distillation can also be carried out in one stage in the sense of partial evaporation of the feed stream.

Process step (b) of the process according to the invention is preferably carried out at an absolute pressure of 0.1 mbar to 100 bar, particularly preferably 1 mbar to 6 bar, in particular 10 mbar to 500 mbar. The distillation is carried out in such a way that the temperature in the bottom of the distillation apparatus is preferably 25 to 250 ° C., particularly preferably 40 to 180 ° C., in particular 60 to 140 ° C. The distillation is carried out in such a way that the temperature at the top of the distillation apparatus is preferably from -15 to 200.degree. C., particularly preferably from 5 to 150.degree. C., in particular from 10 to 100.degree. In a particularly preferred embodiment of the process according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom of the distillation device.

In a particularly preferred embodiment of the present invention, the distillation of stream 1 carried out in process step (b) takes place under pressure and temperature conditions at which the isomerization catalyst present in the mixture is less active than in process step (a) or inactive.

In a preferred embodiment of the present invention, stream 3 obtained in process step (b), which contains the at least one isomerization catalyst, is at least partially returned to process step (a).

In a further embodiment of the method according to the invention, method steps (a) and (b) take place in the same device. It is also possible that stream 3, which contains the at least one isomerization catalyst, is not removed from process step (b) and remains in the common device of process steps (a) and (b).

Alternatively, it is also possible for stream 3 originating from process step (b), which contains the at least one isomerization catalyst, to be used, at least in part, for producing the starting material stream used according to the invention in process step (e). In process step (e), this at least one isomerization catalyst then functions as a hydrocyanation catalyst.

Process step (c)

In process step (c), stream 2 is distilled. Here, a stream 4 is obtained as the top product, which is enriched with respect to stream 2 in (Z) -2-methyl-2-butenenitrile in relation to the sum of all pentenenitriles contained in stream 2. In addition, a stream 5 is obtained as the bottom product, which is depleted from stream 2 of (Z) -2-methyl-2-butenenitrile in relation to the sum of all pentenenitriles contained in stream 2.

Process step (c) can be carried out in any suitable device known to those skilled in the art. Equipment suitable for distillation, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, such as sieve plate columns, Bell-bottom columns, packed columns, packed columns, which can also be operated as dividing wall columns. These distillation devices are each equipped with suitable devices for evaporation, such as falling film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, as well as devices for condensing the vapor stream. The distillation can advantageously be carried out in several, such as two or three, apparatuses in a single apparatus. The distillation can also be carried out in one stage in the sense of partial evaporation of the feed stream.

Process step (c) of the process according to the invention is preferably carried out at an absolute pressure of 0.1 mbar to 100 bar, particularly preferably 1 mbar to 6 bar, in particular 10 mbar to 500 mbar. The distillation is carried out in such a way that the temperature in the bottom of the distillation apparatus is preferably 25 to 250 ° C., particularly preferably 40 to 180 ° C., in particular 60 to 140 ° C. The distillation is carried out in such a way that the temperature at the top of the distillation apparatus is preferably from -15 to 200.degree. C., particularly preferably from 5 to 150.degree. C., in particular from 10 to 100.degree. In a particularly preferred embodiment of the process according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom of the distillation device. In a particularly preferred embodiment of the process according to the invention, process steps (b) and (c) are carried out together in a distillation apparatus, stream 3, which contains the at least one isomerization catalyst, as bottom product, stream 4, the (Z) -2- Containing methyl-2-butenenitrile as top product and stream 5, which contains 3-pentenenitrii and 2-methyl-3-butenenitrile, can be obtained on a side draw of the column.

In a further preferred embodiment of the process according to the invention, process steps (a), (b) and (c) are carried out together in a distillation device. Stream 4, which contains (Z) -2-methyl-2-butenenitrile, is obtained as the top product. Stream 5, which contains 3-pentenenitrile and 2-methyl-3-butenenitrile, is obtained on a side draw of the distillation column. In this embodiment, the isomerization catalyst preferably remains in the bottom of the distillation column.

Process step (d)

The stream 5 obtained in process step (c), which contains 3-pentenenitrile and 2-methyl-3-butenenitrile, is then transferred to a further distillation device. In this distillation device, stream 5 is separated into a 3-pentenenitrile stream, which is taken off as the bottom product, and a 2-methyl-3-butenenitrile stream, which is taken off at the top.

Process step (d) can be carried out in any suitable device known to the person skilled in the art. Equipment suitable for distillation, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, such as sieve plate columns, Bell-bottom columns, packed columns, packed columns, which can also be operated as dividing wall columns. These distillation units are each equipped with suitable devices for evaporation, such as falling film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, and with devices for condensing the vapor stream. The distillation can advantageously be carried out in several, such as two or three, apparatuses in a single apparatus. The distillation can also be carried out in one stage in the sense of partial evaporation of the feed stream.

The absolute pressure in process step (d) is preferably 0.001 to 100 bar, particularly preferably 0.01 to 20 bar, in particular 0.05 to 2 bar. The distillation is carried out so that the temperature in the bottom of the distillation device is preferably 30 to 250 ° C., particularly preferably 50 to 200 ° C., in particular 60 to 180 ° C. The distillation is carried out so that the condensation temperature on Head of the distillation device is preferably -50 to 250 ° C, particularly preferably 0 to 180 ° C, in particular 15 to 160 ° C.

In a particularly preferred embodiment of the process according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom of the distillation device

In a particularly preferred embodiment of the process according to the invention, process step (d) and process step (g) are carried out in the same distillation apparatus. The currents 6 and 12 and 7 and 13 coincide. Furthermore, in this preferred embodiment, stream 5 is fed directly into the common device of process steps (d) and (g). The feed points of streams 5 and 11 can be the same or different in the case of a distillation column as the distillation device.

In a further embodiment of the process according to the invention, process steps (c) and (g) are carried out in a common distillation column, process step (d) being omitted, stream 2 from process step (b) and stream 11 from process step (f) in process step ( g) are carried out in process step (g), stream 4 as the top product, containing (Z) -2-methyl-2-butenenitrile, stream 12 as the bottom product, containing 3-pentenenitrile and stream 13 as a side draw stream, comprising 2 -Methyl-3-butenenitrile can be obtained.

In the process according to embodiment I according to the invention, it is possible for stream 2 to be returned directly to process step (g) and for the educt stream to be fed directly into process step (c), a stream 5a from process step (c) being fed into the isomerization of Process step (a) is returned.

Alternatively, it is also possible to return stream 2 directly to process step (g) and to drive the feed stream into process step (c), stream 5 from process step (c) being returned to process step (f).

Alternatively, it is also possible for stream 2 to be returned directly to process step (g) and for the educt stream to be moved into process step (c) and for stream 5 from process step (c) to be returned to process step (e). Embodiment II

Another object of the present invention is a process for the preparation of 3-pentenenitrile according to an embodiment II, which is characterized by the following process steps:

(a ') Isomerization of a feed stream containing 2-methyl-3-butenenitrile over at least one dissolved or dispersed isomerization catalyst to a stream 1', the 3-pentenenitrile, 2-methyl-3-butenenitrile, the at least one isomerization catalyst and (Z) contains -2-methyl-2-butenenitrile,

(b ') Distillation of stream 1' to give a stream 2 ', which contains (Z) -2-methyl-2-butenenitrile, 2-methyl-3-butenenitrile and is returned to the isomerization step (a'), a stream 3 'as bottom product, which contains the at least one isomerization catalyst and is returned to isomerization step (a'), and a stream 4 ', which contains 3-pentenenitrile, at a side draw of the distillation column.

The starting material stream which is used in process step (a ') of the process according to the invention in accordance with embodiment II can be obtained by the processes described above for producing the starting material stream for the process according to the invention in accordance with embodiment I.

The same conditions apply to process step (a ') according to embodiment II as to process step (a) according to embodiment I, in particular with regard to the catalyst complex used and the free ligand.

The absolute pressure in process step (b ') is preferably 0.001 to 100 bar, particularly preferably 0.01 to 20 bar, in particular 0.1 to 2 bar. The distillation is carried out in such a way that the temperature in the bottom of the distillation apparatus is preferably 25 to 250 ° C., particularly preferably 40 to 180 ° C., in particular 60 to 140 ° C. The distillation is carried out in such a way that the condensation temperature at the top of the distillation apparatus is preferably from -50 to 250 ° C., particularly preferably from 0 to 150 ° C., in particular from 10 to 100 ° C.

A partial discharge of stream 2 'may be indicated in order to avoid leveling up of (Z) -2-methyl-2-butenenitrile. The residual current is returned in step (a '). In a variant of the present process according to embodiment II, the feed stream is led into process step (b ') instead of in process step (a'). Stream 2 ', which leaves process step (b') in the process according to embodiment II according to embodiment II, can optionally be subjected to a distillation in a further optional process step (c '). This preferably forms a stream 5 'enriched in (Z) -2-methyl-2-butenenitrile and a stream 6' depleted in (Z) -2-methyl-2-butenenitrile, stream 5 'preferably being used in process step ( a ') is reduced.

Process step (c ') which may be carried out can also be carried out in the apparatus of process step (a'), in which case a distillation device is used in process step (a '), in the bottom of which the isomerization reaction takes place, via the bottom of the distillation apparatus Stream 1 'is withdrawn and stream 6' rich in (Z) -2-methyl-2-butenenitrile is withdrawn via the top of the distillation apparatus.

According to the invention, 3-pentenenitrile is obtained in the processes according to embodiment I and II. For the purposes of the present invention, the term 3-pentenenitrile means a single isomer of 3-pentenenitrile or a mixture of two, three, four or five different such isomers. The isomers are cis-2-pentenenitrile, trans-2-pentenenitrile, cis-3-pentenenitrile, trans-3-pentenenitrile, 4-pentenenitrile or mixtures thereof, preferably cis-3-pentenenitrile, trans-3-pentenenitrile, 4-pentenenitrile or their mixtures, which are referred to in the context of the present invention both individually and in a mixture as 3-pentenenitrile.

Advantages are associated with the method according to the invention. In an integrated process for the production of adiponitrile, for example, the recycling of unreacted 2-methyl-3-butenenitrile from the isomerization is economically necessary because the degree of conversion of 2-methyl-3-butenenitrile to 3-pentenenitrile by the thermal dynamic equilibrium is limited. The recycle requires that (Z) -2-methyl-2-butenenitrile, which levels up in the 2-methyl-3-butenenitrile circuit, is separated off. In the process according to the invention, the separation is carried out by distillation to separate 2-methyl-3-butenenitrile and (Z) -2-methyl-2-butenenitrile, preferably only after step (a) in step (c) has been carried out, in order to selectively lose valuable products to minimize.

The method according to the invention according to a preferred embodiment of embodiment I is explained in more detail with reference to FIG. 1:

Hydrogen cyanide and 1,3-butadiene are fed into a reactor R1 in the presence of a nickel (0) catalyst. Hydrocyanation takes place in the reactor with the formation of a stream 8. This stream 8 contains 3-pentenenitrile, 2-methyl-3-butenenitrile, the hydrocanization catalyst and unreacted 1,3-butadiene. Then stream 8 is transferred to a distillation column K1, in the overhead 1,3-butadiene (stream 9) is removed from stream 8. A stream 10 which contains the hydrocyanation catalyst is obtained in the bottom in the distillation column K1. At the side draw of the distillation column K1, a stream 11 is obtained which contains 3-pentenenitrile and 2-methyl-3-butenenitrile. This stream 11 is then transferred to a distillation column K2.

In the distillation column K2, the stream 11 is separated into a stream 12 which contains 3-pentenenitrile and a stream 13 which contains 2-methyl-3-butenenitrile.

Stream 13 is then transferred to an isomerization apparatus R2. In this isomerization apparatus R2, the 2-methyl-3-butenenitrile contained in stream 13 is isomerized over an isomerization catalyst. Stream 1 originating from this isomerization contains 3-pentenenitrile, 2-methyl-3-butenenitrile, (Z) -2-methyl-2-butenenitrile and the isomerization catalyst.

This stream 1 is then separated in a distillation apparatus K3. Stream 3 is formed, which contains the isomerization catalyst (bottom). Stream 2 is removed from the top of the distillation apparatus K3. This stream 2 contains 3-pentenenitrile, (Z) -2-methyl-2-butenenitrile and 2-methyl-3-butenenitrile. This stream 2 is then transferred to a distillation column K4.

In this distillation column K4, stream 2 is separated into (Z) -2-methyl-2-butenenitrile, which was formed during the isomerization (stream 4). In addition, stream 5 is obtained in the bottom of distillation column K4, which contains 3-pentenenitrile and 2-methyl-3-butenenitrile. This stream 5 is transferred to the distillation column K2, the 3-pentenenitrile being obtained from stream 5 in the distillation column.

The streams 9 and 10 can be returned completely, partially or not at all to the reactor R1. The same applies to stream 3 in the direction of reactor R2. These variants are not shown in Figure 1.

The method according to the invention according to a preferred embodiment of embodiment II is explained in more detail with reference to FIG. 2:

In a reactor R1, hydrogen cyanide and 1,3-butadiene are fed in the presence of a nickel (0) catalyst. Hydrocyanation takes place in the reactor with the formation of a stream 8. This stream 8 contains 3-pentenenitrile, 2-methyl-3-butenenitrile, the hydrocanization catalyst and unreacted 1,3-butadiene. Stream 8 is then transferred to a distillation column K1 in which 1,3-butadiene is removed from stream 8 overhead (stream 9). A stream 10 which contains the hydrocyanation catalyst is obtained in the bottom in the distillation column K1. At the side draw of the distillation column K1, a stream 11 is obtained which contains 3-pentenenitrile and 2-methyl-3-butenenitrile. This stream 11 is then transferred to an isomerization device R2.

Isomerization catalyst (stream 3 ') and 2-methyl-3-butenenitrile (stream 2'), each originating from the distillation column K2, are additionally introduced into the isomerization device R2. Isomerization takes place in the isomerization device R2. The resulting stream 1 'is then transferred to the distillation device K2, in which the stream 1' is separated into a stream 2 '(2-methyl-3-butenenitriI) which is recycled to R2, a stream 3' (isomerization catalyst) which is recycled into R2 and into a stream 4 'containing 3-pentenenitrile.

By supplying a stream containing isomerization catalyst to R2, any necessary discharges from stream 3 'can be compensated for, so that the Ni (0) content in R2 remains constant.

Streams 9 and 10 can be returned completely, partially or not at all to reactor R1.

These return and discharge variants are not shown in FIG. 2. Embodiment III

In embodiment III, hydrocyanation and isomerization Ni (O) catalysts of such ligands are used which catalyze process steps a *) and e *).

The nickel (0) complexes which are preferably used as the catalyst and which contain phosphorus-containing ligands and / or free phosphorus-containing ligands are preferably homogeneously dissolved nickel (0) complexes.

The phosphorus-containing ligands of the nickel (0) complexes and the free phosphorus-containing ligands are preferably selected from the group of the mono- or bidentate phosphines, phosphites, phosphinites and phosphonites, more preferably the mono- or bidentate phosphites, phosphinites and phosphonites the mono- or bidentate phosphites and phosphonites, in particular the monodentate phosphites, phosphinites and phosphonites, very particularly preferably the monodentate phosphites and phosphonites. These phosphorus-containing ligands preferably have the formula I:

P (X ¹ R ¹ ) (X ² R ² ) (X ³ R ³ ) (I)

According to the invention, X ¹ , X ² , X ^{3 are} independently oxygen or a single bond. If all of the groups X ¹ , X ² and X ³ stand for individual bonds, then compound I represents a phosphine of the formula P (R ¹ R ² R ³ ) with those for R ¹ , R ² and R ^{3 mentioned} in this description Meanings.

If one of the groups X ¹ , X ² and X ^{3 stands} for a single bond and two for oxygen, compound I represents a phosphonite of the formula P (OR ¹ ) (OR ² ) (R ³ ) or P (R ¹ ) (OR ² ) (OR ³ ) or P (OR ¹ ) (R ² ) (OR ³ ) with the meanings given for R ¹ , R ² and R ³ in this description.

In one embodiment, all of the groups X ¹ , X ² and X ^{3 should} stand for oxygen, so that compound I is a phosphite of the formula P (OR) (OR ² ) (OR ³ ) with those for R ¹ , R ² and R ³ represents meanings mentioned below.

According to the invention, R ¹ , R ² , R ³ independently of one another represent identical or different organic radicals. R ¹ , R ² and R ³ are, independently of one another, alkyl radicals, preferably having 1 to 10 carbon atoms, such as methyl, ethyl, n-propyl, i-propyl, n-butyl, i-butyl, s-butyl, t-butyl, Aryl groups, such as phenyl, o-tolyl, m-tolyl, p-tolyl, 1-naphthyl, 2-naphthyl, or hydrocarbyl, preferably having 1 to 20 carbon atoms, such as 1,1'-biphenol, 1,1'- Binaphthol into consideration. The groups R ¹ , R ² and R ³ can be connected to one another directly, that is to say not only via the central phosphorus atom. The groups R ¹ , R ² and R ³ are preferably not directly connected to one another.

In one embodiment, groups R ¹ , R ² and R ³ are selected from the group consisting of phenyl, o-tolyl, m-tolyl and p-tolyl. In one embodiment, a maximum of two of the groups R ¹ , R ² and R ^{3 should be} phenyl groups. In another embodiment, a maximum of two of the groups R ¹ , R ² and R ^{3 should be} o-tolyl groups.

As compounds I, those of the formula I a

(o-Tolyl-O-) _w (m-Tolyl-O-) _x (p-ToIyI-O-) _y (Phenyl-O-) _z P (I a)

Such compounds I a are, for example, (p-tolyl-O -) (phenyl-O-) ₂ P, (m-tolyl-O -) (phenyl-O-) ₂ P, (o-tolyl-O-) (phenyl -O-) ₂ P, (p-tolyl-O-) ₂ (phenyl-O-) P, (m-tolyl-O-) ₂ (phenyl-O-) P, (o-TolyI-O-) ₂ (Phenyl-O-) P, (m-tolyl-O -) (p-tolyl-O) (Phenyl-O-) P, (o-To! Yl-O -) (p-tolyl-O -) ( Phenyl-O-) P, (o-tolyl-O -) (m-tolyl-O -) (phenyl-O-) P, (p-tolyl-O-) ₃ P, (m-tolyl-O-) (p-tolyl-O-) ₂ P, (o-tolyl-O -) (p-tolyl-O-) ₂ P, (m-tolyl-O-) ₂ (p-tolyl-O-) P, ( o-tolyl

O-) ₂ (p-tolyl-O-) P, (o-tolyl-O -) (m-tolyl-O -) (p-tolyl-O) P, (m-tolyl-O-) ₃ P, (o-tolyl-O -) (m-tolyl-O-) ₂ P (o-tolyl-O-) ₂ (m-tolyl-O-) P, or mixtures of such compounds.

Mixtures containing (m-tolyl-O-) ₃ P, (m-tolyl-O-) ₂ (p-tolyl-O-) P, (m-toiyl-O -) (p-tolyl-O-) ₂ P and (p-tolyl-O-) ₃ P can be obtained, for example, by reacting a mixture containing m-cresol and p-cresol, in particular in a molar ratio of 2: 1, as is obtained in the working up of petroleum by distillation, with a phosphorus trihalide, such as phosphorus trichloride , receive.

In one embodiment, the phosphites of the formula I b described in more detail in DE-A 199 53 058 are suitable as phosphorus-containing ligands:

P (OR ¹ ) _x (OR ² ) _y (OR ³ ) _z (OR ⁴ ) _p (I b)

With

R ¹ : aromatic radical with a CrC ₁₈ alkyl substituent in the o-position to the oxygen atom that connects the phosphorus atom to the aromatic system, or with an aromatic substituent in the o-position to the oxygen atom that connects the phosphorus atom to the aromatic system, or with an aromatic system fused in the o-position to the oxygen atom which connects the phosphorus atom to the aromatic system,

R ² : aromatic radical with a CrC ₁₈ alkyl substituent in the m-position to the oxygen atom that connects the phosphorus atom with the aromatic system, or with an aromatic substituent in the m-position to the oxygen atom that connects the phosphorus atom with the aromatic system connects, or with an aromatic system fused in the m-position to the oxygen atom which connects the phosphorus atom to the aromatic system, the aromatic radical in the o-position to the oxygen atom which connects the phosphorus atom to the aromatic system carries a hydrogen atom, more aromatic A residue with a CC ₁₈ alkyl substituent in the p-position to the oxygen atom that connects the phosphorus atom to the aromatic system or with an aromatic substituent in the p-position to the oxygen atom that connects the phosphorus atom to the aromatic system, the aromatic residue bears a hydrogen atom in the o-position to the oxygen atom that connects the phosphorus atom to the aromatic system,

R A. aromatic radical which, in the o-, m- and p-position to the oxygen atom which connects the phosphorus atom to the aromatic system, bears other substituents than those defined for R ¹ , R ² and R ³ , the aromatic radical bears a hydrogen atom in the o-position to the oxygen atom that connects the phosphorus atom to the aromatic system,

x: 1 or 2,

The radical R ² is m-tolyl, m-ethyl-phenyl, mn-propyl-phenyl, m-isopropyl-phenyl, mn-butyl-phenyl, m-sec-butyl-phenyl, m-tert -Butyl-phenyl-, (m-PhenyΙ) -phenyl or 2-naphthyl groups preferred.

Particularly preferred phosphites of the formula Ib are those in which R ^{1 is} the o-isopropylphenyl radical, R ^{2 is} the m-tolyl radical and R ^{3 is} the p-tolyl radical with the indices mentioned in the table above; also those in which R ^{1 is} the o-tolyl radical, R ^{2 is} the m-tolyl radical and R ^{3 is} the p-tolyl radical with the indices specified in the table; furthermore those in which R ^{1 is} the 1-naphthyl radical, R ^{2 is} the m-tolyl radical and R ^{3 is} the p-tolyl radical with the indices specified in the table; also those in which R ^{1 is} the o-tolyl radical, R ^{2 is} the 2-naphthyl radical and R ^{3 is} the p-tolyl radical with the indices specified in the table; and finally those in which R ^{1 is} the o-isopropylphenyl radical, R ^{2 is} the 2-naphthyl radical and R ^{3 is} the p-tolyl radical with the indices given in the table; as well as mixtures of these phosphites.

Phosphites of formula I b can be obtained by

b) the said dihalophosphoric acid monoester is reacted with an alcohol selected from the group consisting of R ¹ OH, R ² OH, R ³ OH and R ⁴ OH or mixtures thereof to give a monohalophosphoric acid diester and

c) the monohalophosphoric diester mentioned is reacted with an alcohol selected from the group consisting of R ¹ OH, R ² OH, R ³ OH and R ⁴ OH or mixtures thereof to give a phosphite of the formula I b.

The implementation can be carried out in three separate steps. Two of the three steps can also be combined, i.e. a) with b) or b) with c). Alternatively, all of steps a), b) and c) can be combined with one another. Suitable parameters and amounts of the alcohols selected from the group consisting of R ¹ OH, R ² OH, R ³ OH and R ⁴ OH or their mixtures can easily be determined by a few simple preliminary tests.

The phosphites Ib can also be used as a ligand in the form of a mixture of different phosphites Ib. Such a mixture can occur, for example, in the production of the phosphites Ib.

It is also possible that the phosphorus-containing ligand is multidentate, in particular bidentate. Then the ligand used has, for example, formula II

on what mean

R ²¹ , R ²² independently of one another are identical or different, individual or bridged organic radicals,

Y bridge group.

In one embodiment, X ¹¹ , X ¹² , X ¹³ , X ²¹ , X ²² , X ²³ can represent oxygen. In such a case, the bridging group Y is linked to phosphite groups. In another embodiment, X ¹¹ and X ¹² oxygen and X ^{13 may be} a single bond or X ¹¹ and X ¹³ oxygen and X ¹² may be a single bond, so that the phosphorus atom surrounded by X ¹¹ , X ¹² and X ^{13 is the} central atom of a phosphonite. In such a case, X ²¹ , X ²² and X ²³ oxygen or X ²¹ and X ²² oxygen and X ²³ a single bond or X ²¹ and X ²³ oxygen and X ²² a single bond or X ²³ oxygen and X ²¹ and X ²² a single bond or X ²¹ oxygen and X ²² and X ^{23 represent} a single bond or X ²¹ , X ²² and X ^{23 represent} a single bond, so that the phosphorus atom surrounded by X ²¹ , X ²² and X ²³ preferably represents a phosphite, phosphonite, phosphinite or phosphine a phosphonite.

In another embodiment, X ¹³ oxygen and X ¹¹ and X ^{12 may be} a single bond or X ¹¹ oxygen and X ¹² and X ^{13 may be} a single bond, so that the phosphorus atom surrounded by X ¹¹ , X ¹² and X ^{13 is the} central atom of a phosphonite. In such a case, X ²¹ to X ²² and X ²³ is oxygen or X ²³ oxygen and X ²¹ and X ²² or X ²¹ oxygen and X ²² and X ²³ or X ^21, X ²² and X ²³ represent a single bond, a single bond, a single bond, so that the phosphorus atom surrounded by X ²¹ , X ²² and X ^{23 can be the} central atom of a phosphite, phosphinite or phosphine, preferably a phosphinite.

In another embodiment, X ¹¹ , X ¹² and X ^{13 can represent} a single bond, so that the phosphorus atom surrounded by X ¹¹ , X ¹² and X ^{13 is the} central atom of a phosphine. In such a case, X ²¹ , X ²² and X ²³ oxygen or X ²¹ , X ²² and X ^{23 represent} a single bond, so that the phosphorus atom surrounded by X ²¹ , X ²² and X ^{23 is the} central atom of a phosphite or phosphine, preferably a phosphine, can be.

Suitable bridging groups Y are preferably substituted, for example with CC ₄ -alkyl, halogen, such as fluorine, chlorine, bromine, halogenated alkyl, such as trifluoromethyl, aryl, such as phenyl, or unsubstituted aryl groups, preferably those having 6 to 20 carbon atoms in the aromatic system , in particular pyrocatechol, bis (phenol) or bis (naphthol).

The radicals R ¹ and R ¹² can independently represent the same or different organic radicals. R ¹¹ and R ¹² are advantageously aryl radicals, preferably those having 6 to 10 carbon atoms, which may be unsubstituted or mono- or polysubstituted, in particular by CC alkyl, halogen, such as fluorine, chlorine, bromine, halogenated alkyl, such as trifluoromethyl, aryl, such as phenyl, or unsubstituted aryl groups.

The radicals R ²¹ and R ²² can independently represent the same or different organic radicals. R ²¹ and R ²² are advantageously aryl residues, preferably those with 6 to 10 carbon atoms, which can be unsubstituted or mono- or polysubstituted, in particular by CC ₄ alkyl, halogen, such as fluorine, chlorine, bromine, halogenated alkyl, such as trifluoromethyl, aryl, such as phenyl, or unsubstituted aryl groups.

In one embodiment, the compounds of the formula I, II, III, IV and V mentioned in US Pat. No. 5,723,641 are suitable. In one embodiment, the compounds of the formula I, II, IM IV, V, VI and VII mentioned in US Pat. No. 5,512,696 and the compounds used in Examples 1 to 31 are suitable. In one embodiment, the compounds of the formula I, II, III, IV, V, VI, VII, VIII, IX, X, XI, XII, XIII, XIV and XV mentioned in US Pat. No. 5,821,378, which are described in Examples 1 to 73 used connections, into consideration.

In one embodiment, the compounds of the formula I, II, III, IV, V and VI mentioned in US Pat. No. 5,512,695, the compounds used there in Examples 1 to 6 are suitable. In one embodiment, the compounds of the formula I, II, IM, IV, V, VI, VII, VIII, IX, X, XI, XII, XIII and XIV mentioned in US Pat. No. 5,981,772, the compounds used there in Examples 1 to 66 , into consideration.

In one embodiment, the compounds mentioned in US Pat. No. 6,127,567 and the compounds used there in Examples 1 to 29 are suitable. In one embodiment, the compounds of the formula I, II, III, which are mentioned in US Pat. No. 6,020,516,

IV, V, VI, VII, VIII, IX and X, the compounds used there in Examples 1 to 33, into consideration. In one embodiment, the compounds mentioned in US Pat. No. 5,959,135 and the compounds used there in Examples 1 to 13 come into consideration.

In one embodiment, the compounds of the formula I, II and IM mentioned in US Pat. No. 5,847,191 are suitable. In one embodiment, the compounds mentioned in US Pat. No. 5,523,453, which are there in the formulas 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 13, 14, 15, 16, 17, 18 , 19, 20 and 21 connections shown. In one embodiment, the compounds mentioned in WO 01/14392 come there, in the formula there

V, VI, VII, VIII, IX, X, XI, XII, XIII, XIV, XV, XVI, XVII, XXI, XXII, XXIII compounds considered.

In one embodiment, the compounds mentioned in WO 98/27054 are suitable. In one embodiment, the connections mentioned in WO 99/13983 fertilize into consideration. In one embodiment, the compounds mentioned in WO 99/64155 are suitable.

In one embodiment, the compounds mentioned in German patent application DE 100 380 37 come into consideration. In one embodiment, the compounds mentioned in German patent application DE 10046025 come into consideration. In one embodiment, the compounds mentioned in German patent application DE 101 50285 come into consideration.

In one embodiment, the compounds mentioned in German patent application DE 101 502 86 come into consideration. In one embodiment, the compounds mentioned in German patent application DE 102 071 65 come into consideration. In a further embodiment of the present invention, the phosphorus-containing chelate ligands mentioned in US 2003/0100442 A1 come into consideration.

In a further embodiment of the present invention, the phosphorus-containing chelate ligands mentioned in the unpublished German patent application file number DE 103 50999.2 dated October 30, 2003 come into consideration.

In a particularly preferred embodiment of the process according to the invention, the phosphorus-containing ligand of the nickel (0) complex and / or the free phosphorus-containing ligand is selected from the phosphites of the formula Ib

P (OR ¹ ) _x (OR ² ) _y (OR ³ ) _z (OR ⁴ ) _p (I b)

wherein R ¹ , R ² and R ^{3 are} independently selected from o-isopropyl-phenyl, m-tolyl and p-tolyl, R ^{4 is} phenyl; x is 1 or 2 and y, z, p are independently 0, 1 or 2 with the proviso that x + y + z + p = 3; and their mixtures, ie mixtures of 2 or more, preferably 2 to 10, particularly preferably 2 to 6, of the compounds of the formula Ib.

In an embodiment III, the process is characterized by the following process steps:

(a *) Isomerization of a feed stream containing 2-methyl-3-butenenitrile over at least one dissolved or dispersed isomerization catalyst to a stream 1 which contains the at least one isomerization catalyst, 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z) contains -2-methyl-2-butenenitrile, (b *) Distillation of stream 1 to give a stream 2 as overhead product which contains 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z) -2-methyl-2-butenenitrile, and a stream 3 as bottom product which contains at least one isomerization catalyst,

(C *) distillation of stream 2 to give a stream 4 as the top product, which is enriched with respect to stream 2 in (Z) -2-methyl-2-butenenitrile, based on the sum of all pentenenitriles in stream 2, and a stream 5 as bottom product which is enriched with respect to stream 2 in 3-pentenenitrile and 2-methyl-3-butenenitrile, based on the sum of all pentenenitriles in stream 2,

(d *) Distillation of stream 5 to give a stream 6 as the bottom product which contains 3-pentenenitrile and a stream 7 as the top product which contains 2-methyl-3-butenenitrile.

(h *) catalyst regeneration to increase the nickel (0) content of the partial streams 14 from stream 3 or 16 from stream 10 to produce your own stream 18,

(i *) optionally with the addition of a diluent F to stream 18 to produce stream 19,

Q *) Extraction of stream 18, if necessary stream 19, with respect to the catalyst components and / or interfering component (s) by adding a dinitrile stream 20 and a hydrocarbon stream 21 to produce two immiscible phases 22 and 23, stream 22 being the predominant part of the catalyst components and stream 23 contains the major part of the interference component (s),

(k *) separation of the hydrocarbon by distillation from the catalyst components from stream 22 to produce a stream 25 which contains the majority of the catalyst components and, if appropriate, partial or complete recycling of stream 25 to process steps (a *) or (e * ).

reactant stream

In process step (a *) an isomerization of a feed stream which contains 2-methyl-3-butenenitrile takes place on at least one isomerization catalyst.

In a special embodiment of the process according to the invention, the educt stream can be obtained by the following process steps: (e *) Hydrocyanation of 1,3-butadiene over at least one hydrocyanation catalyst using hydrogen cyanide to obtain a stream 8 which contains the at least one hydrocyanation catalyst, 3-pentenenitrile, 2-methyl-3-butenenitrile, 1,3-butadiene and residues of hydrogen cyanide .

(f) Single or multiple distillation of stream 8 to obtain stream 9 which contains 1,3-butadiene, stream 10 which contains the at least one hydrocyanation catalyst and stream 11 which contains 3-pentenenitrile and 2-methyl Contains -3-butenenitrile,

(g *) Distillation of stream 11 to give a stream 12 as the bottom product which contains 3-pentenenitrile and a stream 13 as the top product which contains 2-methyl-3-butenenitrile.

Process step e *)

In process step (e *), for the preparation of the educt stream, a hydrocyanation of 1,3-butadiene is first carried out on at least one hydrocyanation catalyst using hydrogen cyanide, giving a stream 8 which comprises the at least one hydrocyanation catalyst, 3-pentenenitrile, 2-methyl-3-butenenitrile and contains unreacted 1,3-butadiene.

Process step (e *) can be carried out in any suitable apparatus known to the person skilled in the art. Conventional apparatuses are therefore suitable for the reaction, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 20, John Wiley & Sons, New York, 1996, pages 1040 to 1055, such as stirred tank reactors, loop reactors, gas circulation reactors, bubble column reactors or tubular reactors, in each case optionally with devices for removing heat of reaction. The reaction can be carried out in several, such as two or three, apparatus.

In a preferred embodiment of the process according to the invention, reactors with backmixing characteristics or cascades of reactors with backmixing characteristics have proven to be advantageous. Cascades from reactors with backmixing characteristics have been found to be particularly advantageous, which are operated in crossflow mode with respect to the metering of hydrogen cyanide.

The hydrocyanation can be carried out in the presence or absence of a solvent. If a solvent is used, the solvent should, at the given reaction temperature and the given reaction pressure, be liquid and inert to the unsaturated compounds and the at least one catalyst. be a goal. In general, hydrocarbons, for example benzene or xylene, or nitriles, for example acetonitrile or benzonitrile, are used as solvents. However, a ligand is preferably used as the solvent.

If the process according to the invention is carried out in semi-batch mode, it is preferred that the catalyst components and 1,3-butadiene are introduced into the reactor while hydrogen cyanide is metered into the reaction mixture over the reaction time.

The reaction is preferably carried out at absolute pressures of 0.1 to 500 MPa, particularly preferably 0.5 to 50 MPa, in particular 1 to 5 MPa. The reaction is preferably carried out at temperatures from 273 to 473 K, particularly preferably 313 to 423 K, in particular at 333 to 393 K. Average residence times of the liquid reactor phase in the range from 0.001 to 100 hours, preferably 0.05 to 20 hours, particularly preferably 0.1 to 5 hours, in each case per reactor, have proven advantageous. In one embodiment, the reaction can be carried out in the liquid phase in the presence of a gas phase and, if appropriate, a solid suspended phase. The starting materials hydrogen cyanide and 1,3-butadiene can each be metered in in liquid or gaseous form.

In a further embodiment, the reaction can be carried out in the liquid phase, the pressure in the reactor being such that all of the starting materials, such as 1,3-butadiene, hydrogen cyanide and the at least one catalyst, are metered in in liquid form and are present in the reaction mixture in the liquid phase. A solid suspended phase can be present in the reaction mixture, which can also be metered in together with the at least one catalyst, for example consisting of degradation products of the catalyst system containing, inter alia, nickel (II) compounds.

In process step (e *), a stream 8 which contains 3-pentenenitrile, 2-methyl-3-butenenitrile, at least one catalyst and unreacted 1,3-butadiene is obtained.

Process step f)

Stream 8, which contains 3-pentenenitrile, 2-methyl-3-butenenitrile, the at least one catalyst and unreacted 1,3-butadiene, is then transferred to a distillation apparatus in process step (f *). In this distillation device, a single or multiple distillation of stream 8 takes place to obtain stream 9 which contains 1,3-butadiene, stream 10 which contains the at least one hydrocyanation catalyst and stream 11 which comprises 3-pentenenitrile and 2 -Methyl-3-butenenitrile contains.

The distillation of process step (f *) can be carried out in two stages, as described in DE-A-102004004720, process steps (b *) and (c *). Process step (f *) can also be distilled according to DE-A-102 004 004729, process steps (b *) and (c *).

The distillation (s) of process step (f *) can be carried out in any suitable apparatus known to the person skilled in the art. Equipment suitable for distillation, as described for example in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, as Sieve tray columns, bubble tray trays, packed columns, packed columns, which can also be operated as dividing wall columns. These distillation devices are each equipped with suitable devices for evaporation, such as falling film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, as well as devices for condensing the vapor stream. The individual distillation NEN can be carried out in several, such as two or three, each advantageously in a single apparatus.

The pressure in process step (f *) is preferably 0.001 to 10 bar, particularly preferably 0.010 to 1 bar, in particular 0.02 to 0.5 bar. The distillation (s) is / are carried out so that the temperature (s) towards the bottom of the Destillationsvor- (s) preferably 30 to 200 ° C, particularly preferably 50 to 150 ^C C, in particular 60 to 120 ° C, is / be. The distillation (s) is / are carried out in such a way that the condensation temperatures at the top of the distillation apparatus are preferably -50 to 150 ° C., particularly preferably -15 to 60 ° C., in particular 5 to 45 ° C. In a particularly preferred embodiment of the process according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom of the distillation device (s).

Stream 11 is then subjected to distillation in a further process step (g *). This distillation can be carried out in any suitable apparatus known to the person skilled in the art. Equipment suitable for distillation, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, such as sieve plate columns, Bell-bottom columns, packed columns, packed columns, which can also be operated as dividing wall columns. These distillation devices are each equipped with suitable devices for evaporation, such as falling film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, and with devices for condensing the vapor stream. The distillation can advantageously be carried out in several, such as two or three, apparatuses in a single apparatus. The distillation can also be carried out in one stage in the sense of partial evaporation of the feed stream.

The pressure in process step (g *) is preferably 0.001 to 100 bar, particularly preferably 0.01 to 20 bar, in particular 0.05 to 2 bar. The distillation is carried out in such a way that the temperature in the bottom of the distillation device is preferably 30 to 250 ° C., particularly preferably 50 to 200 ° C., in particular 60 to 180 ° C. The distillation is carried out in such a way that the condensation temperature at the top of the distillation device is preferably from -50 to 250 ° C., particularly preferably from 0 to 180 ° C., in particular from 15 to 160 ° C. In a particularly preferred embodiment of the process according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom of the distillation device. In process step (g *), a stream 12 is obtained as the bottom product, which contains 1,3-pentenenitrile, and stream 13 as the top product, which contains 2-methyl-3-butenenitrile. Stream 13 is preferably used as a feed stream in the process according to the invention for the production of 3-pentenenitrile.

In a further embodiment of the present invention, it is possible for the educt stream used in process step (a *) according to the invention to correspond to stream 11 of process step (f), so that stream 11 is not separated in process step (g *) ,

Process step (a *)

In process step (a *), the educt stream containing 2-methyl-3-butenenitrile is isomerized over at least one isomerization catalyst. A stream 1 is obtained which contains the isomerization catalyst, unreacted 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z) -2-methyl-2-butenenitrile.

According to the invention, the isomerization is carried out in the presence of a system containing

• Nickel (O) and

• A compound containing trivalent phosphorus containing nickel (O) as a ligand.

The same phosphorus-containing ligands as for the hydrocyanation catalyst used in process step (e *) are used as ligands for the isomerization catalyst. The hydrocyanation catalyst is thus identical to the isomerization catalyst.

The catalyst in process steps (a *) and (e *) is essentially free of Lewis acid, i.e. Lewis acid is never added to the catalyst, preferably the catalyst contains no Lewis acid.

Lewis acid means inorganic or organic metal compounds in which the cation is selected from the group consisting of scandium, titanium, vanadium, chromium, manganese, iron, cobalt, copper, zinc, boron, aluminum, yttrium, Zirconium, niobium, molybdenum, cadmium, rhenium and tin. Examples are ZnBr ₂ , Znl ₂ , ZnCI ₂ , ZnSO ₄ , CuCI ₂ , CuCI, Cu (O ₃ SCF ₃ ) ₂ , CoCI ₂ , Col ₂ , Fel ₂ , FeCI ₃ , FeCI ₂ , FeCl ₂ (THF) _2, TiCl ₄ (THF) _2, TiCl _4, TiCl _3, CITi (Oi-propyl) _3, MnCl _2, SCCI _3l AlCl _3, (C ₈ H ₁₇₎ AlCl _2, (C ₈ H ₁₇ ) ₂ AICI, (iC ₄ H ₉ ) ₂ AlCI, (C ₆ H ₅ ) ₂ AICI, (C ₆ H ₅ ) AICI ₂ , ReCI ₅ , ZrCI ₄ , NbCI _5l VCI ₃ , CrCI ₂ , MoCI _5> YCI ₃ , CdCI ₂ , LaCI ₃ , Er (O ₃ SCF ₃ ) ₃ , Yb (O ₂ CCF ₃ ) ₃ , SmCI ₃ , B (C ₆ H ₅ ) ₃ , TaCI ₅ , RAICI ₂ , R ₂ AICI, RSnO ₃ SCF ₃ and R ₃ B, where R is an alkyl or aryl group, B (C ₆ H ₅ ) ₃ and (C ₆ H ₅ ) ₃ SnX, with X = CF ₃ SO ₃ , CH ₃ C ₆ H ₄ SO ₃ or (C ₆ H ₅ ) ₃ BCN as described for example in US 6,127,567, US 6,171,996, US 6,380,421, US 3,496,217, US 3,496,218, US 4,774,353, US 3,773,809, US 3,496,217 and US 4,874,884.

The isomerization can be carried out in the presence of a liquid diluent,

- For example, an ether, such as diethyl ether, tetrahydrofuran, dioxane, glycol dimethyl ether, anisole, - For example, an ester, such as ethyl acetate, methyl benzoate, or

- For example, a nitrile, such as acetonitrile, benzonitrile, or

- Mixtures of such diluents are carried out.

It has also proven to be advantageous if the isomerization in process step (a *) is carried out in a non-oxidizing atmosphere, such as, for example, under a protective gas atmosphere made of nitrogen or a noble gas, such as argon.

Process step (a *) can be carried out in any suitable apparatus known to the person skilled in the art. Conventional apparatuses are suitable for the reaction, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 20, John Wiley & Sons, New York, 1996, pages 1040 to 1055 are, such as stirred tank reactors, loop reactors, gas circulation reactors, bubble column reactors or tubular reactors. The reaction can be carried out in several, such as two or three, apparatus.

In a further preferred embodiment of the process according to the invention, the isomerization is carried out in at least two reactors connected in series, the first reactor essentially having a stirred tank characteristic and the second reactor being designed such that it essentially has a tube characteristic. In a particularly preferred embodiment of the process according to the invention, the isomerization is carried out in a reactor, the reactor having the characteristic of a stirred tank cascade which corresponds to 2 to 20 stirred tanks, in particular 3 to 10 stirred tanks.

In one embodiment of the process according to the invention, the reaction can be carried out in a distillation apparatus, the isomerization reaction taking place at least in the bottom region of the distillation apparatus. Any distillation apparatus known to the person skilled in the art, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, is suitable Sieve tray columns, bubble tray trays, packed columns, packed columns, which can also be operated as dividing wall columns. These distillation units are each equipped with suitable devices for evaporation, such as falling-film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, as well as devices for condensing the vapor stream. The distillation with the reaction taking place at the same time can advantageously be carried out in several, such as two or three, apparatuses in a single apparatus. The distillation can also be carried out in one stage in the sense of partial evaporation of the feed stream.

Process step (a *) of the process according to the invention is preferably carried out at an absolute pressure of 0.1 mbar to 100 bar, particularly preferably 1 mbar to 16 bar, in particular 10 mbar to 6 bar. The temperature in process step (a *) is preferably 25 to 250 ° C., particularly preferably 30 to 180 ° C., in particular 40 to 140 ° C.

The composition of the withdrawn stream with regard to the molar ratio of 2-methyl-3-butenenitrile to linear pentenenitrile and thus the degree of conversion of 2-methyl-3-butenenitrile used can, depending on the composition of the stream supplied, be determined in a technically simple manner by the temperature, the catalyst concentration, the residence time and the design of the reactor are adjusted. In a preferred embodiment of the process according to the invention, the degree of conversion is adjusted to values in the range of 10 to 99%, particularly preferably 30 to 95%, in particular 60 to 90%, using these measures.

Process step (b *)

In process step (b *), stream 1 obtained in process step (a *) is distilled. The top product obtained is a stream 2 which contains 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z) -2-methyl-2-butenenitrile. In addition, step (b *) a stream 3 obtained as bottom product which contains the at least one isomerization catalyst.

Process step (b *) of the process according to the invention can be carried out in any suitable distillation apparatus known to the person skilled in the art. Equipment suitable for distillation, as described for example in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, as Sieve tray columns, bubble tray trays, packed columns, packed columns, which can also be operated as dividing wall columns. These distillation units are each equipped with suitable devices for evaporation, such as falling-film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation relaxation evaporators, and with devices for condensing the vapor stream. The distillation can advantageously be carried out in several, such as two or three, apparatuses in a single apparatus. The distillation can also be carried out in one stage in the sense of partial evaporation of the feed stream.

Process step (b *) of the process according to the invention is preferably carried out at an absolute pressure of 0.1 mbar to 100 bar, particularly preferably 1 mbar to 6 bar, in particular 10 mbar to 500 mbar. The distillation is carried out in such a way that the temperature in the bottom of the distillation apparatus is preferably 25 to 250 ° C., particularly preferably 40 to 180 ° C., in particular 60 to 140 ° C. The distillation is carried out in such a way that the temperature at the top of the distillation apparatus is preferably from -15 to 200.degree. C., particularly preferably from 5 to 150.degree. C., in particular from 10 to 100.degree. In a particularly preferred embodiment of the process according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom of the distillation device.

In a particularly preferred embodiment of the present invention, the distillation of stream 1 carried out in process step (b *) takes place under pressure and temperature conditions at which the isomerization catalyst present in the mixture is less active than in process step (a *) or inactive.

In a preferred embodiment of the present invention, stream 3 obtained in process step (b *) and containing the at least one isomerization catalyst is at least partially returned to process step (a *).

In a further embodiment of the method according to the invention, method steps (a *) and (b *) take place in the same device. It is also possible that stream 3, which contains the at least one isomerization catalyst, is not removed from process step (b *) and remains in the common device of process steps (a *) and (b *). Process step (c *)

In process step (c *), stream 2 is distilled. Here, a stream 4 is obtained as the top product, which is enriched with respect to stream 2 in (Z) -2-methyl-2-butenenitrile in relation to the sum of all pentenenitriles contained in stream 2. In addition, a stream 5 is obtained as the bottom product, which is depleted from stream 2 of (Z) -2-methyl-2-butenenitrile in relation to the sum of all pentenenitriles contained in stream 2.

Process step (c *) can be carried out in any suitable device known to the person skilled in the art. Equipment suitable for distillation, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, such as Siebboden- columns, bubble-cap trays, packed columns, packed columns, which can also be operated as dividing wall columns. These distillation units are each equipped with suitable devices for evaporation, such as falling-film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, as well as devices for condensing the vapor stream. The distillation can advantageously be carried out in several, such as two or three, apparatuses in a single apparatus. The distillation can also be carried out in one stage in the sense of partial evaporation of the feed stream.

Process step (c *) of the process according to the invention is preferably carried out at an absolute pressure of 0.1 mbar to 100 bar, particularly preferably 1 mbar to 6 bar, in particular 10 mbar to 500 mbar. The distillation is carried out in such a way that the temperature in the bottom of the distillation apparatus is preferably 25 to 250 ° C., particularly preferably 40 to 180 ° C., in particular 60 to 140 ° C. The distillation is carried out in such a way that the temperature at the top of the distillation device is preferably from -15 to 200.degree. C., particularly preferably from 5 to 150.degree. C., in particular from 10 to 100.degree. In a particularly preferred embodiment of the process according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom of the distillation device.

In a particularly preferred embodiment of the process according to the invention, process steps (b *) and (c *) are carried out together in a distillation apparatus, stream 3, which contains the at least one isomerization catalyst, as bottom product, stream 4, the (Z) - Containing 2-methyl-2-butenenitrile, as top product and stream 5, which contains 3-pentenenitrile and 2-methyl-3-butenenitrile, can be obtained on a side draw of the column. In a further preferred embodiment of the process according to the invention, process steps (a *), (b *) and (c *) are carried out together in a distillation device. Stream 4, which contains (Z) -2-methyl-2-butenenitrile, is obtained as the top product. Stream 5, which contains 3-pentenenitrile and 2-methyl-3-butenenitrile, is obtained on a side draw of the distillation column. In this embodiment, the isomerization catalyst preferably remains in the bottom of the distillation column.

Process step (d *)

The stream 5 obtained in process step (c *), which contains 3-pentenenitrile and 2-methyl-3-butenenitrile, is then transferred to a further distillation device. In this distillation device, stream 5 is separated into a 3-pentenenitrile stream, which is taken off as the bottom product, and a 2-methyl-3-butenenitrile stream, which is taken off at the top.

Process step (d *) can be carried out in any suitable device known to the person skilled in the art. Equipment suitable for distillation, as described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 4th Ed., Vol. 8, John Wiley & Sons, New York, 1996, pages 334-348, such as sieve plate columns, Bell-bottom columns, packed columns, packed columns, which can also be operated as dividing wall columns. These distillation units are each equipped with suitable devices for evaporation, such as falling film evaporators, thin-film evaporators, multi-phase spiral tube evaporators, natural circulation evaporators or forced circulation flash evaporators, and with devices for condensing the vapor stream. The distillation can advantageously be carried out in several, such as two or three, apparatuses in a single apparatus. The distillation can also be carried out in one stage in the sense of partial evaporation of the feed stream.

The absolute pressure in process step (d *) is preferably 0.001 to 100 bar, particularly preferably 0.01 to 20 bar, in particular 0.05 to 2 bar. The distillation is carried out so that the temperature in the bottom of the distillation device is preferably 30 to 250 ° C., particularly preferably 50 to 200 ° C., in particular 60 to 180 ° C. The distillation is conducted so that the condensation temperature at the top of the distillation apparatus is preferably from -50 C to 250 ^{° C.,} more preferably 0 to 180 ° C, especially 15 to 160 ° C, is.

In a particularly preferred embodiment of the process according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom of the distillation device In a particularly preferred embodiment of the process according to the invention, process step (d *) and process step (g *) are carried out in the same distillation apparatus. The currents 6 and 12 and 7 and 13 coincide. Furthermore, in this preferred embodiment, stream 5 is fed directly into the common device of process steps (d *) and (g *). The feed points of streams 5 and 11 can be the same or different in the case of a distillation column as the distillation device.

In a further embodiment of the process according to the invention, process steps (c *) and (g *) are carried out in a common distillation column, process step (d *) being omitted, stream 2 from process step (b *) and stream 11 from process step (f *) are carried out in process step (g ^* ), in process step (g *) the stream 4 as top product containing (Z) -2-methyl-2-butenenitrile, the stream 12 as bottom product containing 3-pentenenitrile and the stream 13 can be obtained as a side draw stream containing 2-methyl-3-butenenitrile.

In the method according to the embodiment IM according to the invention, it is possible for the stream 2 to be returned directly to the process step (g *) and for the educt stream to be fed directly into the process step (c *), a stream 5a from process step (c *) ) is returned to the isomerization of process step (a *).

Alternatively, it is also possible to return stream 2 directly to process step (g *) and to drive the feed stream into process step (c *), stream 5 from process step (c *) being returned to process step (f *).

Alternatively, it is also possible for stream 2 to be returned directly to process step (g *) and for the educt stream to be moved into process step (c *) and for stream 5 from process step (c *) to be returned to process step (e *) ,

Process step h *):

Process step h *) includes a process for the preparation of nickel (O) phosphorus ligand complexes containing at least one nickel (0) central atom and at least one phosphorus-containing ligand.

In the following, the terms reductive catalyst synthesis / regeneration and redox catalyst synthesis / regeneration are synonymous.

Step hi *):

A preferred embodiment of process step h *), here referred to as process step hi *), is characterized in that a process obtained by azeotropic distillation dried (previously dry according to Azeodest) water-containing nickel (II) halide is reduced in the presence of at least one phosphorus-containing ligand.

azeotropic

A water-containing nickel (M) halide is used in the azeotropic distillation. Water-containing nickel (II) halide is a nickel halide which is selected from the group of nickel chloride, nickel bromide and nickel iodide, which contains at least 2% by weight of water. Examples of these are nickel chloride dihydrate, nickel chloride hexahydrate, an aqueous solution of nickel chloride, nickel bromide trihydrate, an aqueous solution of nickel bromide, nickel iodide hydrates or an aqueous solution of nickel iodide. In the case of nickel chloride, nickel chloride hexahydrate or an aqueous solution of nickel chloride is preferably used. In the case of nickel bromide and nickel iodide, the aqueous solutions are preferably used. An aqueous solution of nickel chloride is particularly preferred.

In the case of an aqueous solution, the concentration of the nickel (II) halide in water per se is not critical. A proportion of the nickel (II) halide in the total weight of nickel (II) halide and water of at least 0.01% by weight, preferably at least 0.1% by weight, particularly preferably at least 0, has proven advantageous. 25% by weight, particularly preferably at least 0.5% by weight. A proportion of the nickel (II) halide in the total weight of nickel (II) halide and water in the range of at most 80% by weight, preferably at most 60% by weight, particularly preferably at most 40% by weight, has proven advantageous. % proven. For practical reasons, it is advantageous not to exceed a proportion of nickel halide in the mixture of nickel halide and water which gives a solution under the given temperature and pressure conditions. In the case of an aqueous solution of nickel chloride, it is therefore advantageous for practical reasons to choose a proportion of nickel halide in the total weight of nickel chloride and water of at most 31% by weight at room temperature. At higher temperatures, correspondingly higher concentrations can be chosen, which result from the solubility of nickel chloride in water.

The water-containing nickel (M) halide is dried by an azeotropic distillation before the reduction. In a preferred embodiment of the present invention, azeotropic distillation is a process for removing water from the corresponding water-containing nickel (II) halide, to which a diluent is added, the boiling point of which in the case of non-azeotropic formation of the diluent with water under the pressure conditions the distillation mentioned below is higher than the boiling point of water and which is liquid at this boiling point of water or which is an azeotrope or heteroazeotrope with water under the pressure and temperature conditions of the following Distillation forms, and the mixture containing the water-containing nickel (II) halide and the diluent, with separation of water or said azeotrope or said heteroazeotrope from this mixture and to obtain an anhydrous mixture containing nickel (II) - halide and the said diluent is distilled.

In addition to the water-containing nickel (II) halide, the starting mixture can contain further constituents, such as ionic or nonionic, organic or inorganic compounds, in particular those which are homogeneously miscible with the starting mixture or are soluble in the starting mixture.

According to the invention, the water-containing nickel (II) halide is mixed with a diluent whose boiling point is higher than the boiling point of water under the pressure conditions of the distillation and which is liquid at this boiling point of the water.

The pressure conditions for the subsequent distillation are not critical per se. Pressures of at least 10 ^"4 MPa, preferably at least 10 ^{" 3} MPa, in particular at least 5 * 10 ^"3 MPa, have proven advantageous. Pressures of at most 1 MPa, preferably at most 5 * 10 ^{" 1} MPa, in particular at most, have proven advantageous 1.5 * 10 ^"1 MPa.

The distillation temperature is then set depending on the pressure conditions and the composition of the mixture to be distilled. At this temperature the diluent is preferably in liquid form. For the purposes of the present invention, the term diluent is understood to mean both an individual diluent and a mixture of such diluents, and in the case of such a mixture the physical properties mentioned in the present invention relate to this mixture.

Furthermore, the diluent under these pressure and temperature conditions preferably has a boiling point which in the case of not form an azeotrope of the diluent with water higher than that of water, preferably at least 5 ° C, in particular at least 20 ^C C, and preferably at most 200 ^C C, in particular at most 100 ° C.

In a preferred embodiment, diluents can be used which form an azeotrope or heteroazeotrope with water. The amount of diluent is not critical per se to the amount of water in the mixture. It is advantageous to use more liquid diluent than the amounts to be distilled off by the azeotropes, so that excess diluent remains as the bottom product. If a diluent is used which does not form an azeotrope with water, the amount of diluent is not critical per se in relation to the amount of water in the mixture.

The diluent used is in particular selected from the group consisting of organic nitriles, aromatic hydrocarbons, aliphatic hydrocarbons and mixtures of the aforementioned solvents. With regard to the organic nitriles, acetonitrile, propionitrile, n-butyronitrile, n-valeronitrile, cyanocyclopropane, acrylonitrile, crotonitrile, allyl cyanide, cis-2-pentenenitrile, trans-2-pentenenitrile, cis-3-pentenenitrile, trans-3-pentenenitrile 4-pentenenitrile, 2-methyl-3-butenenitrile, Z-2-methyl-2-butenenitrile, E-2-methyl-2-butenenitrile, ethylsuccinonitrile, adiponitrile, methyiglutamitrile or mixtures thereof. With regard to the aromatic hydrocarbons, benzene, toluene, o-xylene, m-xylene, p-xylene! or mixtures thereof can be used. Aliphatic hydrocarbons can preferably be selected from the group of linear or branched aliphatic hydrocarbons, particularly preferably from the group of cycloaliphatics, such as cyclohexane or methylcyclohexane, or mixtures thereof. Cis-3-pentenenitrile, trans-3-pentenenitrile, adiponitrile, methyiglutamitrile or mixtures thereof are particularly preferably used as solvents.

If an organic nitrile or mixtures containing at least one organic nitrile is used as the diluent, it has proven to be advantageous to choose the amount of diluent such that the proportion of the nickel (II) halide in the finished mixture of the total weight of nickel (II) halide and diluent is at least 0.05% by weight, preferably at least 0.5% by weight, particularly preferably at least 1% by weight. \

If an organic nitrile or mixtures containing at least one organic nitrile is used as the diluent, it has proven to be advantageous to choose the amount of diluent such that the proportion of the nic (II) halide in the finished mixture of the total weight of nickel (II) halide and diluent is at most 50% by weight, preferably at most 30% by weight, particularly preferably at most 20% by weight.

According to the invention, the mixture containing the water-containing nickel (II) halide and the diluent is distilled, with the separation of water from this mixture and to obtain an anhydrous mixture containing nickel (M) halide and the said diluent. In a preferred embodiment, the mixture is first prepared and then distilled. In another preferred embodiment, the water-containing nickel halide, particularly preferably the aqueous solution of the nickel halide, gradually increases during the distillation added to the boiling diluent. As a result, the formation of a greasy solid which is difficult to handle in terms of process technology can be substantially avoided.

In the case of pentenenitrile as the diluent, the distillation can advantageously be carried out at a pressure of at most 1 megapascal, preferably 0.5 megapascal.

In the case of pentenenitrile as diluent, the distillation can preferably be carried out at a pressure of at least 1 kPa, preferably at least 5 kPa, particularly preferably 10 kPa.

The distillation can advantageously be carried out by single-stage evaporation, preferably by fractional distillation in one or more, such as 2 or 3, distillation apparatuses. Equipment suitable for distillation for this purpose, such as those described, for example, in: Kirk-Othmer, Encyclopedia of Chemical Technology, 3rd Ed., Vol. 7, John Wiley & Sons, New York, 1979, pages 870-881 , such as sieve tray columns, bubble tray trays, packed columns, packed columns, columns with side take-off or dividing wall columns.

The distillation can be carried out batchwise or continuously.

reduction

The process for the preparation of nickel (0) -phosphorus ligand complexes containing at least one nickel (0) central atom and at least one phosphorus-containing ligand by reduction is preferably carried out in the presence of a solvent. The solvent is in particular selected from the group consisting of organic nitriles, aromatic hydrocarbons, aliphatic hydrocarbons and mixtures of the solvents mentioned above. With regard to the organic nitriles, acetonitrile, propionitrile, n-butyronitrile, n-valeronitrile, cyano cyclopropane, acrylonitrile, crotonitrile, allyl cyanide, cis-2-pentenenitrile, trans-2-pentenenitrile, cis-3-pentenenitrile, trans-3- PentenenitriI, 4-pentenenitrile, 2-methyl-3-butenenitrile, Z-2-methyl-2-butenenitrile, E-2-methyl-2-butenenitrile, ethylsuccinonitrile, adiponitrile, methyiglutamitrile or mixtures thereof. With regard to the aromatic hydrocarbons, benzene, toluene, o-xylene, m-xylene, p-xylene or mixtures thereof can preferably be used. Aliphatic hydrocarbons can preferably be selected from the group of linear or branched aliphatic hydrocarbons, particularly preferably from the group of cycloaliphatics, such as cyclohexane or methylcyclohexane, or mixtures thereof. Cis-3-pentenenitrile, trans-3-pentenenitrile, adiponitrile, methyiglutamitrile or mixtures thereof are particularly preferably used as solvents. An inert solvent is preferably used.

The concentration of the solvent is preferably 10 to 90% by mass, particularly preferably 20 to 70% by mass, in particular 30 to 60% by mass, in each case based on the finished reaction mixture.

In a particular embodiment of the present invention, the solvent is identical to the diluent used in the process according to the invention described above for producing the anhydrous mixture containing the nickel (II) halide and the diluent.

In the process according to the invention, the concentration of the ligand in the solvent is preferably 1 to 90% by weight, particularly preferably 5 to 80% by weight, in particular 50 to 80% by weight.

The reducing agent used in the process according to the invention is preferably selected from the group consisting of metals which are more electropositive than nickel, metal alkyls, electric current, complex hydrides and hydrogen.

If a metal which is more electropositive than nickel is used as the reducing agent in the process according to the invention, this metal is preferably selected from the group consisting of sodium, lithium, potassium, magnesium, calcium, barium, strontium, titanium, vanadium, Iron, cobalt, copper, zinc, cadmium, aluminum, gallium, indium, tin, lead and thorium. Iron and zinc are particularly preferred. If aluminum is used as the reducing agent, it is advantageous if it is preactivated by reaction with a catalytic amount of mercury (II) salt or metal alkyl. Triethylaluminum is preferably used for the preactivation in an amount of preferably 0.05 to 50 mol%, particularly preferably 0.5 to 10 mol%. The reducing metal is preferably finely divided, the term "finely divided" meaning that the metal is used in a particle size of less than 10 mesh, particularly preferably less than 20 mesh.

If a metal which is more electropositive than nickel is used as the reducing agent in the process according to the invention, the amount of metal is preferably 0.1 to 50% by weight, based on the reaction mass.

If metal alkyls are used as reducing agents in the process according to the invention, they are preferably lithium alkyls, sodium alkyls, magnesium alkyls, in particular Grignard reagents, zinc alkyls or aluminum alkyls. Aluminum alkyls, such as trimethyl aluminum, triethyl aluminum, tri-isopropyl aluminum or mixtures thereof, in particular triethyl aluminum, are particularly preferred. The Metal alkyls can be used in bulk or dissolved in an inert organic solvent, such as hexane, heptane or toluene.

If complex hydrides are used as reducing agents in the process according to the invention, preference is given to using metal aluminum hydrides, such as lithium aluminum hydride, or metal borohydrides, such as sodium borohydride.

The molar ratio of the redox equivalents between the nickel (II) source and the reducing agent is preferably 1: 1 to 1: 100, particularly preferably 1: 1 to 1:50, in particular 1: 1 to 1: 5.

In the process according to the invention, the ligand to be used can also be present in a ligand solution which has already been used as a catalyst solution in hydrocyanation reactions such as step e *) or isomerization reactions such as step a *) and which is depleted in nickel (O). Such streams are streams 3 and 10, either partially or in each case independently selected sub-streams 14 (from sub-stream 3) or sub-stream 16 (from sub-stream 10) in stage h *) and the following stages, if appropriate i *), j *) and k *) are driven. The remaining partial streams 15 (from stream 3) and 17 (from stream 10) are not carried out by h *), i *), j *) and k *), but are returned directly to stage a *) or e *) , This "back catalyst solution" generally has the following composition:

2 to 60% by weight, in particular 10 to 40% by weight, of pentenenitrile, 0 to 60% by weight, in particular 0 to 40% by weight of adiponitrile,

0 to 10% by weight, in particular 0 to 5% by weight, of other nitriles,

- 10 to 90 wt .-%, in particular 50 to 90 wt .-% phosphorus-containing ligand and

- 0 to 2 wt .-%, in particular 0 to 1 wt .-% nickel (O).

The free ligand contained in the back catalyst solution can thus be converted back to a nickel (0) complex by the process according to the invention.

In a particular embodiment of the present invention, the ratio of the nickel (II) source to the phosphorus-containing ligand is 1: 1 to 1: 100. Further preferred ratios of the nickel (II) source to the phosphorus-containing ligand are 1: 1 to 1: 3, especially 1: 1 to 1: 2. The method according to the invention can be carried out at any pressure. For practical reasons, pressures between 0.1 bara and 5 bara, preferably 0.5 bara and 1.5 bara, are preferred.

The process according to the invention can be carried out in batch mode or continuously.

In the process according to the invention it is possible to work without an excess of nickel (II) halide or reducing agent, for example zinc, so that it is not necessary to separate them after the nickel (0) complex has formed.

In a particular embodiment of the present invention, the method according to the invention comprises the following method steps:

(1) drying of a water-containing nickel (II) halide by azeotropic distillation,

(2) precomplexing the azeotropically dried nickel (II) halide in a solvent in the presence of a phosphorus-containing ligand, (3) adding at least one reducing agent to the solution or suspension from process step (2) at an addition temperature of 20 to 120 ° C,

(4) stirring the suspension or solution from process step (3) for at a reaction temperature of 20 to 120 ° C.

The pre-complexing temperatures, addition temperatures and reaction temperatures can, independently of one another, be 20 ° C. to 120 ° C. Temperatures of 30 ° C. to 80 ° C. are particularly preferred in the pre-complexing, addition and reaction.

The pre-complexation periods, addition periods and implementation periods can, independently of one another, be 1 minute to 24 hours. The pre-complexation period is in particular 1 minute to 3 hours. The addition period is preferably 1 minute to 30 minutes. The reaction period is preferably 20 minutes to 5 hours.

Process step h ₂ *):

A further preferred embodiment of process step h *), described here as process step h ₂ *), involves increasing the nickel (0) content of streams 14 and 16, for example, by stirring in nickel powder. Free phosphorus Ligand used in streams 14 and 16 as a complexing partner or fresh ligand added.

The catalyst compounds can be made from nickel powder with a suitable halide source as an initiator, such as, for example, a halide or an alkyl-substituted halide of phosphorus, arsenic or antimony, such as CH ₃ PCI ₂ , CH3ASCI2 or CH ₃ SbCI ₂ , or a suitable metal halide Halogen, such as chlorine, bromine or iodine, or the corresponding hydrogen halides or thionyl halide. Metal halides to be used according to the invention are the halides of Cr, Ni, Ti, Cu, Co, Fe, Hg, Sn, Li, K, Ca, Ba, Sc, Ce, V, Mn, Be, Ru, Rh, Pd, Zn, Cd, Al, Th, Zr and Hf. The halide can be chloride, bromide or iodide. Particularly suitable halide sources are PX ₃ , TiX, ZrX ₄ , HfX ₄ or HX, where X is chloride, bromide or iodide. When carrying out the reaction according to the invention, mixtures of 2 or more initiators or catalysts can also be used.

The catalyst regeneration can be carried out discontinuously, e.g. in batch mode analogous to US 3,903,120 or continuously analogous to US 4,416,825 at temperatures from 0 to 200 ° C, preferably 25 to 145 ° C, particularly preferably 50 to 100 ° C. The residence time of the catalyst can be varied within wide limits and is generally between 15 minutes and 10 hours, preferably 20 minutes and 5 hours, particularly preferably 30 minutes and 2 hours.

If method step h ₂ *) is carried out instead of method step f), method steps i *), j *) and k *) can optionally be omitted in whole or in part.

Process step i *):

If necessary, stream 18 can be distilled prior to step i) by e.g. at pressures from 0.1 to 5000, preferably 0.5 to 1000 and in particular 1 to 200 mbar (abs.) and temperatures from 10 to 150, preferably 40 to 100 ° C. - or other suitable measures, for example to 50 to 95 , preferably 60 to 90% of its original volume. In a particularly preferred embodiment, after concentration, this stream contains up to 10% by weight, that is to say 0 to 10% by weight, preferably 0.01 to 8% by weight, of pentenenitriles.

Step i *): adding the non-polar aprotic liquid F

In step i *), a non-polar aprotic liquid F is added to stream 18, whereby a stream 19 is obtained. Liquid means that the compound F is in liquid form at least under the pressure and temperature conditions prevailing in step i *); at other pressure and temperature conditions, F can also be solid or gaseous. Suitable nonpolar (or apolar) aprotic liquid F are all compounds which are liquid under the conditions of step i *) and which catalyze the catalyst, for example the Ni (0) complex with phosphorus-containing ligands and / or the free phosphorus-containing ligands or physically or not significantly change. Compounds suitable as liquid F contain no ionizable proton in the molecule and generally have low relative dielectric constants (ε _r <15) or low electrical dipole moments (μ <2.5 Debye).

Particularly suitable are hydrocarbons, which can be, for example, unhalogenated or halogenated, and - in particular tertiary - amines, and carbon disulfide.

In a preferred embodiment, the liquid F is a hydrocarbon K *. Aliphatic, cycloaliphatic or aromatic hydrocarbons K * are suitable. Suitable aliphatic hydrocarbons are e.g. linear or branched alkanes or alkenes with 5 to 30, preferably 5 to 16, carbon atoms, in particular pentane, hexane, heptane, octane, nonane, decane, undecane and dodecane (in each case all isomers).

Suitable cycloaliphatic hydrocarbons have, for example, 5 to 10 carbon atoms, such as cyclopentane, cyclohexane, cycloheptane, cycloocatane, cyclononane and cyclodecane. Substituted, especially C _1-10 -alkyl-substituted cycloaliphatics such as methylcyclohexane are also suitable. Aromatic hydrocarbons which are preferably suitable are those having 6 to 20 carbon atoms, in particular benzene, toluene, o-, m- and p-xylene, naphthalene and anthracene. It is also possible to use substituted, preferably C 1-6 alkyl-substituted aromatics such as ethylbenzene.

The hydrocarbon K * is particularly preferably selected from the compounds mentioned below for the hydrocarbon K. The hydrocarbon K * is very particularly preferably identical to the hydrocarbon K, i.e. the same hydrocarbon is used for the extraction in step j *) and as liquid F.

Design of adding the liquid

The non-polar aprotic liquid F can be added to stream 18 in conventional mixing devices. Preferably because the process is particularly simple, in step i ^* ) the nonpolar aprotic liquid F is mixed with the stream 18 in a stirred tank or a pumping circuit.

The nonpolar aprotic liquid is preferably intimately mixed with the stream 18. Usual liquid mixers with intensive mixing are suitable as mixing tanks Mixing elements and / or static or movable internals can be provided.

The use of a pumping circuit is also preferred. It is usually operated in such a way that the ratio of pumping quantity to output from the pumping circuit is 0.1: 1 to 1000: 1, preferably 1: 1 to 100: 1 and particularly preferably 2: 1 to 25: 1. As a circulation pump, e.g. Gear pumps or other common pumps. The circulating pump preferably works against an overflow which operates at a defined pressure of e.g. 3 to 10 bar (abs.) Opens.

If the same hydrocarbon is used in step i *) and j *), fresh hydrocarbon can be used in both steps. Likewise, one can continue to use the hydrocarbon used in step i *) in step j *), or recycle the hydrocarbon used in step j *) after step i *) and continue to use it there.

In a very particularly preferred embodiment, the liquid F is a partial stream of the stream 22 (hydrocarbon K enriched with catalyst, see below) which occurs in step j *). This means that part of stream 22 is branched off in step j *) and the branched part is added to stream 18 in step i *). In this embodiment, part of the current 22 is accordingly circulated.

In another, likewise preferred embodiment, the nonpolar aprotic liquid F is metered directly into a residence time section (see below), for example at the beginning thereof.

The liquid F is generally added at temperatures from 0 to 150, preferably 10 to 100 and in particular 20 to 80 ° C., and pressures from 0.01 to 100, preferably 0.1 to 10 and in particular 0.5 to 5 cash (abs.).

The required amount of liquid F can vary within wide limits. It is generally less than the amount of hydrocarbon K used to extract in step j *), but can also be larger. The amount of the liquid F is preferably 0.1 to 200% by volume, in particular 1 to 50% by volume and particularly preferably 5 to 30% by volume, based on the amount of the extract in step j *) used hydrocarbon K.

Optional treatment with ammonia or amine

If step h *) contains a redox regeneration, stream 18 or stream 19 or during step i *) or during step j *) may itself ammonia or a primary res, secondary or tertiary aromatic or aliphatic amine can be added. Aromatic includes alkyl aromatic, and aliphatic includes cycloaliphatic.

It was found that this ammonia or amine treatment changes the catalyst, in particular nickel (0) complex or ligand during extraction (step j *)) in the second phase enriched with dinitriles (stream 23) can be reduced, ie during the extraction, the distribution of the Ni (0) complex or the ligands over the two phases is shifted in favor of the first phase (stream 22). The ammonia or amine treatment improves the catalyst enrichment in stream 22; this means lower catalyst losses in the catalyst circuit and improves the economy of the hydrocyanation.

Accordingly, in this embodiment the extraction is preceded by treatment of stream 18 or stream 19 with ammonia or an amine or takes place during the extraction. Treatment during extraction is less preferred.

It is particularly preferred to add the ammonia or the amine together with the nonpolar aprotic liquid F. In particular, the liquid F and the ammonia or amine are added in the same mixing device.

Monomamines, diamines, triamines or higher functional amines (polyamines) are used as amines. The monoamines usually have alkyl radicals, aryl radicals or arylalkyl radicals with 1 to 30 C atoms; suitable monoamines are e.g. primary amines, e.g. Monoalkylamines, secondary or tertiary amines, e.g. Dialkylamines. Suitable primary monoamines are, for example, butylamine, cyclohexylamine, 2-methylcyclohexylamine, 3-methylcyclohexylamine, 4-methylcyclohexylamine, benzylamine, tetrahydrofurfurylamine and furfurylamine. The secondary monoamines are e.g. Diethylamine, dibutylamine, di-n-propylamine and N-methylbenzylamine are considered. Suitable tertiary amines are, for example, trialkylamines with Ci.io-alkyl radicals, such as trimethylamine, triethylamine or tributylamine.

Suitable diamines are, for example, those of the formula R ¹ -NH-R -NH-R ³ , in which R ¹ , R ² and R ³ independently of one another are hydrogen or an alkyl radical, aryl radical or arylalkyl radical having 1 to 20 carbon atoms. The alkyl radical can be linear or, in particular for R ^2, also cyclic. Suitable diamines are, for example, ethylenediamine, the propylenediamines (1,2-diaminopropane and 1,3-diaminopropane), N-methyl-ethylenediamine, piperazine, tetramethylenediamine (1,4-diaminobutane), N, N'-dimethylethylenediamine, N-ethylethylenediamine, 1,5-diaminopentane, 1,3-diamino-2,2-diethylpropane, 1,3-bis (methylamino) propane, hexamethylenediamine (1,6-diaminohexane), 1,5-diamino-2- methylpentane, 3- (propyiamino) propylamine, N, N'-bis (3-aminopropyl) piperazine, N, N'-bis (3-aminopropyl) piperazine and isophoronediamine (IPDA). Suitable triamines, tetramines or higher-functional amines are, for example, tris (2-aminoethyl) amine, tris (2-aminopropyl) amine, diethylenetriamine (DETA), triethylenetetramine (TE-TA), tetraethylenepentamine (TEPA), isopropylenetriamine, dipropylenetriamine and N, N'- bis (3-aminopropyl-ethylenediamine). Aminobenzylamines and aminohydrazides with 2 or more amino groups are also suitable.

Naturally, mixtures of ammonia with one or more amines or mixtures of several amines can also be used.

Ammonia or aliphatic amines, in particular trialkylamines having 1 to 10 carbon atoms in the alkyl radical, e.g. Trimethylamine, triethylamine or tributylamine, and diamines such as ethylenediamine, hexamethylenediamine or 1,5-diamino-2-methylpentane.

Ammonia alone is particularly preferred, i.e. in addition to ammonia, amine is particularly preferably used. Anhydrous ammonia is especially preferred; water-free means a water content below 1% by weight, preferably below 1000 and in particular below 100 ppm by weight.

The molar ratio of amine to ammonia can be varied within a wide range, generally from 10000: 1 to 1: 10000.

The amount of ammonia or amine used depends, among other things. the type and amount of catalyst, e.g. of the nickel (0) catalyst and / or the ligands, and - if used - according to the type and amount of the Lewis acid which is used as a promoter in the hydrocyanation. The molar ratio of ammonia or amine to Lewis acid is usually at least 1: 1. The upper limit of this molar ratio is generally not critical and is, for example, 100: 1; however, the excess of ammonia or amine should not be so large that the Ni (0) complex or its ligands decompose. The molar ratio of ammonia or amine to Lewis acid is preferably 1: 1 to 10: 1, particularly preferably 1.5: 1 to 5: 1, and in particular about 2: 1. If a mixture of ammonia and amine is used , these molar ratios apply to the sum of ammonia and amine.

The temperature in the treatment with ammonia or amine is usually not critical and is, for example, 10 to 140, preferably 20 to 100 and in particular 20 to 90 ° C. The pressure is usually not critical either.

The ammonia or the amine can be added to the stream 18 in gaseous form, liquid (under pressure) or dissolved in a solvent. Suitable solvents are, for example, nitriles, in particular those which are present in the hydrocyanation, and also aliphatic, cycloaliphatic or aromatic hydrocarbons, such as they are used as extractants in the process according to the invention, for example cyclohexane, methylcyclohexane, n-heptane or n-octane.

The ammonia or amine is added in conventional devices, for example those for introducing gas or in liquid mixers. The solid that precipitates in many cases can either remain in stream 18, i.e. a suspension is fed to the extraction, or separated as described below.

Optional separation of the solids

In a preferred embodiment, solids which precipitate in step i *) of the process are separated from stream 19 before extraction (step j *)).

In many cases, this allows the extraction performance of the method according to the invention to be further improved, since the solids often reduce the separation performance of the extraction devices. In addition, it was found that, in some cases, the removal of solids before the extraction significantly reduced or even completely suppressed the undesired formation of sludge.

The solid separation is preferably designed in such a way that solid particles with a hydraulic diameter greater than 5 μm, in particular greater than 1 μm and particularly preferably greater than 100 nm, are separated.

Customary methods can be used for the separation of solids, for example filtration, crossflow filtration, centrifugation, sedimentation, classification or preferably decanting, for which purpose common devices such as filters, centrifuges or decanters can be used.

The temperature and pressure during the separation of solids are usually not critical. For example, you can work in the temperature or pressure ranges mentioned above or below.

The solids can be separated off before, during or after the - optional - treatment of stream 18 or stream 19 with ammonia or amine. Separation during or after the ammonia or amine treatment is preferred, and is particularly preferred thereafter.

If the solids are removed during or after the ammonia or amine treatment, the solids are mostly compounds of ammonia or amine with the Lewis acid used or the promoter which are poorly soluble in stream 18. If, for example, ZnCl _{2 is used} , ZnCl '2 NH ₃ which is essentially sparingly soluble precipitates during the ammonia treatment. If the solids are separated off before the ammonia or amine treatment or if there is no treatment with ammonia or amine at all, the solids are generally nickel compounds of the oxidation state + ^| |, for example nickel (II) cyanide or similar cyanide-containing nickel (II) compounds, or around Lewis acids or their compounds. The compounds mentioned can precipitate, for example, because their solubility has been reduced, for example by a change in temperature.

Optional dwell time

The stream 19 as a discharge from step i *) can be transferred directly to step j *), for example through a pipeline. This means that the mean residence time of stream 19 in the pipeline is less than 1 min.

However, in a preferred embodiment, the method according to the invention is characterized in that the stream 19 is passed through a dwell time after step i *) and before step j *). The residence time is therefore after the addition of the liquid F and before the extraction.

Suitable dwell times are e.g. Pipelines, static mixers, stirred or non-stirred containers or container cascades, as well as combinations of these elements. The dwell time is preferably dimensioned and designed such that the average dwell time of the stream 19 in the dwell time is at least 1 min, preferably at least 5 min.

The optional solids separation described above can also be carried out in the residence time zone. The dwell time serves as a calming zone in which the solid can settle. In this way, the dwell time acts like a decanter or crossflow filter. It can be provided with devices for conveying and / or discharging solids.

As mentioned, in a preferred embodiment the non-polar aprotic liquid F is metered directly into the residence time segment, for example at the beginning thereof. In this embodiment, it is particularly preferred to choose a residence time section which ensures intimate mixing of stream 18 and liquid F. As has also already been described, the residence time segment can cause a phase separation of the current 19.

The residence time is generally at temperatures from 0 to 200, preferably 10 to 150 and in particular 20 to 100 ° C., and pressures of 0.01 to 100, preferably 0.1 to 10 and in particular 0.5 to 5 bar (abs .), operated. In a preferred embodiment of the invention, the flow rate of the stream 19 in all the pipelines used in the method according to the invention is at least 0.5, in particular at least 1 and particularly preferably at least 2 m / s.

The stream 19 obtained in step a) is extracted in step j *), if appropriate after the treatment with ammonia or amines and / or after the solids removal and / or after passing through the residence time section.

Process step j *):

process principle

The process according to the invention is suitable for the extractive purification of Ni (0) complexes, which contain phosphorus-containing ligands and / or free phosphorus-containing ligands, in stream 19 or, if appropriate, stream 18, if step i *) is not carried out, by adding a C6- Dinitrils such as adiponitrile (ADN), 2-methylglutaronitrile (MGN) or 2-ethylsuccinonitrile (ESN) with regard to the interfering component (s), which an increased formation of C5-mononitriles such as E-2-methyl-2-butenenitrile and not accessible from the hydrocyanation / or trigger Z-2-methyl-2-butenenitrile.

In addition, the catalyst losses in the extraction are reduced by supplying a hydrocarbon K in stream 21 to an inlet point which is closer to the outlet point of the extract than to the inlet point of feed stream 18 or 19. The feed point of the dinitrile (stream 20) is closer to the drain point of the raffinate than the feed point of the feed stream 18 or 19. Here is to be understood as closer in the sense of the number of theoretical separation levels between two points. Between the feed points of streams 18 and 19 and 21 there are generally 0 to 10, preferably 1 to 7, theoretical extraction (separation) stages (back-extraction zone for the catalyst); 1 to 10, preferably 1 to 5, theoretical extraction (separation) stages (cleaning zone with respect to interfering component (s)) generally lie between the feed points of streams 18 or 19 and 20.

As a rule, a first phase is formed at a temperature T (in ° C.) [raffinate;

Stream 22], which is enriched with respect to the stream 18 at the said Ni (0) complexes or ligands, and a second phase [extract; Stream 23; enriched interfering component (s)], which is enriched with dinitriles compared to stream 18. The first phase is usually the easier phase, i.e. the upper phase, and the second phase is the heavier phase, i.e. the lower phase. After the phase separation, the upper phase preferably contains between 50 and 99% by weight, particularly preferably between 60 and 97% by weight, in particular between 80 and 95% by weight, of the hydrocarbon used for the extraction.

The Lewis acid, which is optionally present in the feed stream of the extraction (namely when generating the redox catalyst regeneration in process step hi *)) preferably remains largely and particularly preferably completely in the lower phase. Here completely means that the residual concentration of the Lewis acid in the upper phase is preferably less than 1% by weight, particularly preferably less than 0.5% by weight, in particular less than 500 ppm by weight.

The removal of the interfering component (s) improves the process selectivity since less C5 mononitriles which are not accessible to the hydrocyanation are formed (reduction of incorrect isomerizations).

A particular advantage of embodiment III is that dinitriles such as ADN, MGN, ESN, which form in small quantities in process step e *) and thus accumulate in stream 10, are at least partially discharged with the lower phase of the extraction.

Another particular advantage of using process step j *) is that butadiene containing stabilizer can be used as starting material in process step e *). Such a stabilizer can be, for example, tert-butyl catechol. This stabilizer is carried out over the lower phase of the extraction. Thus, no catalyst-damaging concentrations of the stabilizer in the catalyst circuit can be leveled.

Another particular advantage is that in process step h *) a redox regeneration of the catalyst to increase the Ni (0) value according to hf) can be carried out, since the Lewis acid formed is discharged through the lower phase of the extraction becomes. This Lewis acid would otherwise lead to increased dinitrile formation in the first hydrocyanation (process step e *).

The lower phase of the extraction can be prepared in a suitable manner so that the dinitriles contained therein can be used again as feed for the extraction. Such processing can e.g. done by distillation (DE-A-102004 004683; stream 7 from step c)).

Organization of the extraction

The extractive tasks can preferably be solved by using a countercurrent extraction column with a back-extraction zone. However, there are also Combinations of the same type of any suitable apparatus known to the person skilled in the art, such as countercurrent extraction columns, mixer-settler cascades or combinations of mixer-settler cascades with columns, for example a series connection of two countercurrent extraction columns (for example one for cleaning with respect to Interfering component (s), the other for the back extraction of the catalyst). It is particularly preferred to use countercurrent extraction columns which are equipped in particular with sheet metal packs as dispersing elements. In a further particularly preferred embodiment, the extraction is carried out in countercurrent in compartmentalized, stirred extraction columns.

Regarding the direction of dispersion, in a preferred embodiment of the process the hydrocarbon is used as the continuous phase and the stream 18 of the hydrocyanation is used as the disperse phase. This usually shortens the phase separation time and reduces the build-up of debris. However, the reverse dispersion direction, ie stream 18 as a continuous and hydrocarbon as a disperse phase, is also possible. The latter applies in particular if the formation of sludge is reduced or completely suppressed by prior solid separation (see below), higher temperature during the extraction or phase separation or use of a suitable hydrocarbon. Usually the dispersion direction which is more favorable for the separation performance of the extraction device is chosen.

The following ratios of the feeds are set in the extraction: stream 20 to the sum of stream 18 or 19 and stream 21 in the range from 0.01 to 10 kg / kg, preferably 0.05 to 5 kg / kg. Stream 21 to stream 20 in the range of 0.05 to 20 kg / kg, preferably 1 to 10 kg / kg. Stream 21 to stream 18 or 19 in the range from 0.05 to 20 kg / kg, preferably 0.5 to 8 kg / kg.

The absolute pressure during the extraction is preferably 10 kPa to 1 MPa, particularly preferably 50 kPa to 0.5 MPa, in particular 75 kPa to 0.25 MPa (absolute).

The extraction is preferably carried out at a temperature of -15 to 120 ° C, in particular 20 to 100 ° C and particularly preferably 30 to 80 ° C. It was found that the muck formation is lower at a higher temperature of the extraction.

Design of phase separation

The phase separation can also be viewed as the last part of the extraction, in terms of space and time, depending on the design of the apparatus. A wide pressure, concentration and temperature range can usually be selected for phase separation, and the parameters which are optimal for the particular composition of the reaction mixture can easily be determined by a few simple preliminary tests. The temperature T during phase separation is usually at least 0 ° C., preferably at least 10 ° C., particularly preferably at least 20 ° C. Usually it is at most 120 ° C, preferably at most 100 ° C, particularly preferably at most 95 ° C. For example, the phase separation is carried out at 0 to 100 ° C., preferably 60 to 95 ° C. It was found that the build-up of lump is lower at a higher temperature of the phase separation.

The pressure during phase separation is generally at least 1 kPa, preferably at least 10 kPa, particularly preferably 20 kPa. As a rule, it is at most 2 MPa, preferably at most 1 MPa, particularly preferably at most 0.5 MPa absolute.

The phase separation time, that is to say the time period from the mixing of the stream 18 with the hydrocarbon (extractant) to the formation of a uniform upper phase and a uniform lower phase, can vary within wide limits. The phase separation time is generally 0.1 to 60, preferably 1 to 30 and in particular 2 to 10 minutes. When carrying out the process according to the invention on an industrial scale, a phase separation time of at most 15, in particular at most 10, minutes is usually technically and economically sensible.

It has been found that the phase separation time is advantageously reduced in particular when using long-chain aliphatic alkanes such as n-heptane or n-octane as the hydrocarbon K.

The phase separation can be carried out in one or more devices known to those skilled in the art for such phase separations. In an advantageous embodiment, the phase separation can be carried out in the extraction device, for example in one or more mixer-settler combinations or by equipping an extraction column with a settling zone.

The phase separation gives two liquid phases, one phase of which has a higher proportion of the Nicke! (0) complex with phosphorus-containing ligands and / or free phosphorus-containing ligands, based on the total weight of this phase, than the other phase or other phases , The other phase is enriched in the interference component (s).

dinitrile

Stream 20, which is fed as a feed stream for extraction, contains predominantly dinitriles, preferably C6 dinitriles, particularly preferably adiponitrile (ADN), 2-methylglutaronitrile (MGN), 2-ethylsuccinonitrile (ESN) or mixtures of those. The flow of dinitriles in this stream is preferably greater than 50% by weight, particularly preferably greater than 70% by weight, particularly preferably greater than 90% by weight. Processes for the production of dinitriles, in particular C6 dinitriles, are known per se. One possible method of this type is described in DE-A-102004004683. Streams of C6 dinitriles produced in this way, in particular streams 15, 16 and 17 from process step h) from DE-A-102004 004683, are generally suitable for being used here as stream 20.

Dinitriles are preferably added to the extent that phase separation takes place in the extraction stage k *).

Hydrocarbon

The hydrocarbon is the extractant. It preferably has a boiling point of at least 30 ° C, particularly preferably at least 60 ° C, in particular at least 90 ° C, and preferably at most 140 ° C, particularly preferably at most 135 ° C, in particular at most 130 ^C , in each case at a pressure of 10 ⁵ Pa absolute.

A hydrocarbon, in the sense of the present invention a single hydrocarbon as well as a mixture of such hydrocarbons, is particularly preferred for the separation, in particular by extraction, of adiponitrile from a mixture containing adiponitrile and the catalyst containing Ni (0), be used, which has a boiling point in the range between 90 ° C and 140 ° C. The adiponitrile can advantageously be obtained from the mixture obtained after the separation according to this process by distillative separation of the hydrocarbon, the use of a hydrocarbon having a boiling point in the range mentioned making it particularly economical and technically simple to separate by the possibility of condensing the distilled off Hydrocarbon allowed with river water.

Suitable hydrocarbons are described, for example, in US Pat. No. 3,773,809, column 3, lines 50-62. Preferably comes a hydrocarbon selected from cyclohexane, methylcyclohexane, cycloheptane, n-hexane, n-heptane, isomeric heptanes, n-octane, iso-octane, isomeric octanes such as 2,2,4-trimethylpentane, ice and trans- Decalin or mixtures thereof, in particular from cyclohexane, methylcyclohexane, n-heptane, isomeric heptanes, n-octane, isomeric octanes such as 2,2,4-trimethylpentane, or mixtures thereof. Cyclohexane, methylcyclohexane, n-heptane or n-octane are particularly preferably used.

N-Heptane or n-octane are very particularly preferred. With these hydrocarbons, the undesirable formation of dross is particularly low. Mulm is understood to be an area of incomplete phase separation between the upper and lower phases, usually a liquid / liquid mixture in which solids can also be dispersed. Excessive debris formation is undesirable because it hinders extraction and the extraction device may be flooded by the debris, which means that it can no longer perform its separation task.

The hydrocarbon used is preferably anhydrous, where anhydrous means a water content of less than 100, preferably less than 50, in particular less than 10 ppm by weight. The hydrocarbon can be dried by suitable processes known to those skilled in the art, for example by adsorption or azeotropic distillation. Drying can take place in a step upstream of the method according to the invention.

Process step k *):

In process step (k *), stream 22 is distilled to obtain stream 25 containing at least one catalyst and stream 24 containing the extractant.

This process step essentially serves to recover the catalyst and the extractant.

Process step (k *) can be carried out in any suitable apparatus known to the person skilled in the art. Process step k *) is preferably distilled in one or more evaporation stages and rectification columns / distillation columns.

Structured sheet metal packing, structured fabric packing, bell bottoms, dual-flow trays or fillings of packing elements or combinations of two or more of these classes of separating internals are preferably used as internals for the rectification columns / distillation columns. The rectification column distillation column of process step k *) can be carried out with one or more liquid or gaseous side draws. The rectification column distillation column from process step k *) can be carried out as a dividing wall column with one or more gaseous or liquid side draws present.

The one or more evaporator stages or the rectification column / distillation column of process step k *) can in particular be equipped with falling film evaporators, thin-film evaporators, natural circulation evaporators, forced circulation flash evaporators and multi-phase spiral tube evaporators. In a further embodiment of the process according to the invention, at least one of the evaporator units from process step k *) is operated with a divided bottom, the first major bottom of the relevant evaporator stage being used to drive the circulating stream, which is generally large in relation to the bottom draw stream, to the evaporator, the liquid effluent stream from the evaporator, however, does not return directly to the sump, but collects it in a second sump, which is separate from the first sump, receives the sump draw stream from the second sump and allows the remaining excess from the evaporator recycle stream to overflow into the first sump, with the sump draw flow off a mixture is obtained in the second sump, which is depleted in low boilers compared to the withdrawal from the first sump.

The absolute pressure in process step k *) is preferably 0.001 to 2 bar (a), particularly preferably 0.01 to 0.5 bar (a), in particular 0.09 to 0.12 bar (a). The distillation is carried out such that the temperature in the bottom of the distillation apparatus is preferably 40 to 150 ° C., particularly preferably 70 to 120 ° C., in particular 80 to 100 ° C. The distillation is carried out in such a way that the temperature at the top of the distillation apparatus is preferably from -15 to 100.degree. C., particularly preferably from 0 to 60.degree. C., in particular from 20 to 50.degree. In a particularly preferred embodiment of the method according to the invention, the aforementioned temperature ranges are maintained both at the top and in the bottom.

When the extractant is separated off in order to recover the catalyst according to process step k *), 3-pentenenitrile can optionally be added as an intermediate boiler for distillation. This solvent change may have the advantage that an effective depletion of the extractant from the high-boiling catalyst stream becomes possible at evaporator temperatures that are low enough not to thermally damage the nickel catalyst used, especially when using chelate ligands, and thermally when using monodentate ligands to protect, the pressure is still high enough to be able to condense the comparatively low-boiling extractant at the top of the evaporator stage or distillation column at conventional cooling water temperatures of 25 to 50 ° C compared to the catalyst components. The solvent change may also have the advantage that the fluidity and the single-phase nature of the catalyst solution is ensured, since, depending on the temperature and residual extractant content, catalyst components may crystallize out without the addition of 3-pentenenitrile. In this case, 3-pentenenitrile, which, for example, is difficult to remove from the extracting agents cyclohexane or methylcyclohexane or heptane or n-heptane, depending on the pressure conditions, or cannot be removed completely at all due to minimum vapor pressure azeotrope formation, preferably in a proportion of up to 10% by weight preferably up to 5% by weight, in particular up to 1% by weight, based on the total amount of extractant feed stream to the extraction column in process step j *) does not interfere with the process according to the invention.

In a preferred embodiment of the process according to the invention, the stream 24 obtained in process step k *) and containing the extracting agent is at least partially returned to the extraction step j *). Here, the recycled stream 24 is optionally dried before the extraction step j *), so that the water content in this stream is preferably less than 100 ppm by weight, particularly preferably less than 50 ppm by weight, in particular less than 10 ppm by weight, is.

In a further preferred embodiment of the process according to the invention, the stream 25 obtained in process step k *) and containing the catalyst is at least partially recycled into the hydrocyanation of process step e *) or into the isomerization of process step a *). In a preferred embodiment of the method according to the invention, the proportion of extractant in stream 25 is preferably less than 10% by weight, particularly preferably less than 5% by weight, in particular less than 1% by weight, based on the total amount from stream 25.

Preferred embodiments of the catalyst flow through process steps a *) to k *) are described below with the aid of schemes 1 to 5. Process step i *) is not included in schemes 1 to 5, but can be carried out between h *) and j *). Schemes 1 to 5 exemplarily describe method step h *) in the embodiment as method step hi *). Alternatively, the embodiment can also be carried out as method step h ₂ *). In these cases, the nickel (ll) chloride would be replaced by nickel powder, the reducing agent (Red.) As well as the Lewis acid (LS) are eliminated. ADN is synonymous with dinitrile currents; Heptane synonymous with hydrocarbons as an extractant. Cat. Means each catalyst complex plus free ligand. The dashed lines in schemes 1 to 5 indicate optional bypass partial flows of the catalyst flows.

A special embodiment of the method with regard to the flow of catalyst is shown in Scheme 1. Accordingly, the catalyst-carrying stages are combined in a single catalyst circuit. Starting from the first hydrocyanation, the sequence of the process stages is e *), f *). a *). b *), c *), h *), possibly i *), j *), k *), before feeding e *) again. If necessary, a partial stream of the catalyst can be recycled past stages h *), i *), j *) and k *) directly into e *). Process step a *) is fed here with an unseparated mixture of 2-methyl-3-butenenitrile and 3-pentenenitrile, i.e. d *) or g *) is executed after a *).

A further special embodiment of the method with regard to the catalyst flow is shown in Scheme 2. Accordingly, the catalyst-carrying stages are in summarized in a single catalyst circuit. Starting from the first hydrocyanation, the sequence of the process steps is e ^* ), f ^* ), a *), b *), c *), h *), if appropriate i *). j *). K *) _ι ^before e *) is fed again. If necessary, a partial stream of the catalyst can be recycled past stages h *), i *), j *) and k *) directly into e ^* ). Process step a *) is fed with 2-methyl-3-butenenitrile depleted of 3-pentenenitrile, ie d *) or g *) is carried out before a *).

A further special embodiment of the process with regard to the flow of catalyst is shown in scheme 3. Accordingly, a catalyst stream is circulated through stages e *) and f). A partial stream is discharged from this stream and used as catalyst feed for stage a *). This stream is then completely, if necessary partially, fed back into e *) through stages b *), c *), h *), if appropriate i *), j *) and k *). The isomerization stage a *) is fed with 2-methyl-3-butenenitrile depleted with respect to 3-pentenenitrile, i.e. d *) or g *) is executed before a *). Likewise, d * or g * can also be executed after a *.

A further special embodiment of the method with regard to the catalyst flow is shown in Scheme 4. Accordingly, two catalyst circuits are built. Catalyst circuit 1 contains stages e *) and f *), catalyst circuit 2 stages a *), b *), c *). From both streams, partial streams, if appropriate also the total catalyst streams in each case, are driven via stages h *), if appropriate i *), j *) and k *), in order to clean the catalyst from interfering components and / or the Ni (0 ) To increase the content. The portion of catalyst circuit 2 driven by the extraction is preferably greater than that of catalyst circuit 1. If appropriate, the entire stream from catalyst circuit 2 is passed through the extraction. The two catalyst circuits are only coupled to one another via stages h *), optionally i *), j *) and k *). The distribution of the stream from k *) for feeding a *) or e *) generally corresponds to the ratio of the feed streams to h *) from a *) and e *). The isomerization step a *) is fed with 2-methyl-3-butenenitrile depleted with respect to 3-pentenenitrile, i.e. d *) or g *) is executed before a *). Likewise, d * or g * can also be executed after a *.

A further particular embodiment of the method with regard to the catalyst flow is shown in Scheme 5. Accordingly, a catalyst circuit is operated via stages a *), b *), c *), h *), optionally i *), j *) and k *). A partial stream is drawn off from this catalyst circuit before h *) and the first hydrocyanation e *) is thus carried out. The current is returned to h *) via f *). If necessary, the return can also be made directly to a *). A partial stream of the isomerization catalyst circuit can also be recycled from c *) directly to a *). The isomerization stage a *) is fed with 2-methyl-3-butenenitrile depleted with respect to 3-pentenenitrile, ie d *) or g *) is carried out before a *). Likewise, d * or g * can also be executed after a *. The present invention is explained in more detail with reference to the examples shown below.

A u s r u n g s b e i s p i e l e

The following abbreviations are used in the examples:

Hydrogen cyanide: hydrogen cyanide

T3PN: trans-3-pentenenitrile

C3PN: cis-3-pentenenitrile

4PN: 4-pentenenitrile

E2M2BN: (E) -2-methyl-2-butenenitrile

T2PN: trans-2-pentenenitrile

C2PN: cis-2-pentenenitrile

ADN: adiponitrile

MGN: methyiglutamitrile

VSN: valeric acid nitrile

VCH: 4-vinylcyclohexene

BD: 1,3-butadiene

TBC: tert-butyl catechol

C2BU: cis-2-butene

LS: Lewis acid

In the examples, the process steps are given in a chronological order and thus differ from the description in the description and in the claims. Unspecified data in% or ppm are% by weight or ppm by weight.

Example 1 :

Example 1 is illustrated using FIG. 3.

In example 1, a catalyst system based on nickel (0) complexes with a mixture of ligands is used for the hydrocyanation of butadiene. The ligand mixture for hydrocyanation contains about 60 mol% of tri (m / p-tolyl) phosphite and 40 mol% of the chelate phosphonite 1:

In a step (1), the following streams are fed into a loop reactor R1 of 25 l volume, which is equipped with a nozzle, pulse exchange tube, external pump circuit and in a heat exchanger in the pump circuit for dissipating the reaction energy and is tempered to 357 K:

(1) 10 kg / h of liquid unstabilized hydrogen cyanide freed from water by distillation,

(2) 22 kg / h commercial BD containing 0.25% C2BU treated by contact with alumina to remove water and TBC stabilizer,

(3) 8 kg / h of recycled BD from K2a in step (2) (stream 9), so that the total BD feed to the reactor R1 is a stream of 30 kg / h containing 90% BD, 5% C2BU and 5% 1 -Butene is obtained

(4) 21 kg / h of nickel (0) catalyst solution, obtained as described in this example below as stream 10a from column K2b

The stream 8 (63 kg / h) drawn off from the reactor R1 contains a total of 11% BD and C2BU, corresponding to a conversion of 79% BD, and a total of 63% pentenenitriles, 31% T3PN, 29% 2M3BN and small amounts of Z2M2BN and E2M2BN and other pentenenitrile isomers (T2PN, C2PN, C3PN, 4PN), as well as the catalyst components and catalyst degradation products and MGN.

Stream 8 is fed in a step (2) to a distillation column K2a, which is operated with a rectifying and stripping section and is equipped with a falling film evaporator and a separate sump, and contains column internals with structured packing which produce 10 theoretical plates. Column K2a is operated at the head with a direct condenser which consists of a column section equipped with a structured packing with a total collecting cup, pumping circuit and external heat exchanger. The column K2a is operated at an absolute top pressure of 2.0 bar, 288 K top temperature and 363 K bottom draw temperature. Stream 9 is obtained at the top of column K2a and, as described at the beginning, is metered into the reactor R1 as a recycle stream. The reflux ratio at the top of column K2a is adjusted so that stream 9 contains approximately 100 ppm 2M3BN.

59 kg / h of a stream 1b which contains 2.9% BD, 4.6% C2BU, 67% pentenenitriles and additionally the catalyst constituents are obtained at the bottom of column K2a. C2BU is significantly enriched compared to BD compared to the inflow.

In step (2), stream 1b is fed into a distillation column K2b which is operated in the stripping mode and is equipped with falling film evaporator, top condenser with post-condenser and column internals with structured packing which generate 10 theoretical plates. The column is operated at an absolute top pressure of 150 mbar, 329 K top temperature and 373 K bottom draw temperature. The vapor stream from the column is partially condensed at 308 K and treated with a post-condenser at 263 K. The BD stream 2c depleted in this way by 2M3BN and other pentenenitriles is compressed in a compressor V2 to an absolute pressure of 1.2 bar. The compressed gas stream is largely condensed at 279 K to obtain a stream 2e (5 kg / h), a partial stream 2d (47 Nl / h, containing 44% C2BU) being disposed of in gaseous form. Stream 2e is returned in liquid form to the condensate collection container in column K2a.

At column K2b, stream 11 is obtained in a gaseous side draw (40 kg / h), containing approx. 100 ppm BD, 46% 2M3BN and 48% T3PN and to a lesser extent E2M2BN and Z2M2BN along with other pentenenitrile isomers. The position of the side draw is selected such that the component 2M3BN is depleted in the stream 10 obtained via the sump in relation to T3PN under the side draw in a stripping section.

13 kg / h of a catalyst stream are fed into the column K2b and, as described in Example 1 according to the German patent application with the title “Process for the Production of Dinitriles” from BASF AG (B03 / 0525), as a bottom draw from the column K4 from step (4) is obtained, containing a total of 73% pentenenitriles, 0.5% Ni (0), 18% ligand mixture and about 5% ADN.

The catalyst stream 10 containing 0.5% Ni (0), about 100 ppm 2M3BN and 73% remaining pentenenitriles is obtained at the bottom of column K2b. Stream 10 is split into partial stream 10a (21 kg / h), which is returned to reactor R1. The other part (10b) (5.4 kg / h) is fed to a regeneration according to DE-A-103 51 002 in order, after regeneration, for example in the hydrocyanation of 3-pentenenitrile as in Example 1 according to DE-A-102004004683 described to be used. The stream 11 is moved in a step (3) to a distillation column K3, which is equipped with a circulation evaporator and overhead condenser and with a structured packing, which generate 30 theoretical plates. The column K3 is operated at an absolute top pressure of 180 mbar, 345 K top temperature and 363 K bottom draw temperature.

39 kg / h of recycle stream 5 from column K5 are fed into column K3 in step (5), containing 54% T3PN, 23% 2M3BN and 16% Z2M2BN and small amounts of further pentenenitrile isomers.

Over the top of the column K3, 40 kg / h of a stream 13 are obtained, containing 10% T3PN, 68% 2M3BN, 16% Z2M2BN and in total 0.1% BD and C2BU and small amounts of other pentenenitrile isomers (T2PN, C2PN, C3PN , 4PN).

39 kg / h of stream 12 are obtained at the bottom of column K3, comprising a total of 97% of T3PN, C3PN and 4PN and small amounts of other pentenenitrile isomers (T2PN, C2PN) and about 100 ppm of 2M3BN and about 1% of E2M2BN.

In Example 1, a catalyst system based on nickel (0) complexes with a mixture of ligands is used for the isomerization of 2M3BN to T3PN. The ligand mixture for isomerization (hereinafter referred to as isomerization ligand) contains mixed phosphite ligands of the class P (OR) (OR ') (OR ") with statistically distributed R, R', R" from the group m-tolyl, p-tolyl, o -Isopropylphenyl, where about 40 mol% of the sum of the radicals R, R ', R "are o-isopropylphenyl radicals. Such ligand mixtures are used in the reaction of a mixture of m- and p-cresol with a ratio of 2: 1 of m-cresol versus p-cresol and a stoichiometrically adjusted amount of o-isopropylphenol with a phosphorus trihalide.

In a step (4), the stream 13 is fed together with a catalyst recycle stream 3a and a catalyst supplementary stream into a reactor R2, in the form of a tubular reactor which is heated to 393 K. The sum of the recirculation catalyst and the fresh catalyst is fed into the R2 reactor 56 kg / h of a mixture with 20% T3PN, 5% 2M3BN and other pentenenitrile isomers, 55% isomerization ligand and 0.5% nickel (O) and a low content of catalyst degradation products.

The product from reactor R2 is 96 kg / h of stream 1, containing 34% T3PN, 12.3% 2M3BN and small amounts of other pentenenitrile isomers (T2PN, C2PN, C3PN, 4PN), corresponding to a conversion of 60% 2M3BN.

In a step (5), stream 1 is fed into a distillation column K5, which is operated as a rectification column and is equipped with a falling film evaporator, overhead condenser and reflux condenser. flow divider, gaseous side discharge in the bottom area of the column and column internals with structured packing, which generate 30 theoretical plates. The column is operated at an absolute top pressure of 250 mbar, 353 K top temperature and 373 K bottom draw temperature.

The recovered catalyst stream 3 (56 kg / h) is obtained in column K5, containing 20% T3PN in addition to other pentenenitriles, about 5% MGN and 0.5% Ni (0) and 54% isomerization ligand. A small part of stream 3 is discharged as stream 3b to limit the level of catalyst deactivation components and MGN. To supplement the discharged amount of catalyst, so much fresh catalyst, containing 15% T3PN in addition to other pentenenitrile isomers, 1% Ni (0) and 80% isomerization ligand, is metered in so that the Ni (0) content in the catalyst feed to the reactor R2 is 0.5 % is held.

In column K5, a stream 4 is obtained overhead (0.8 kg / h), containing a total of 0.5% BD and C2BU, 50% 2M3BN, 41% Z2M2BN, and small amounts of vinylcyclohexene (VCH), which on the one hand in traces is contained in the feed material BD and on the other hand is formed in small amounts in the hydrocyanation of butadiene and ultimately levels up in the 2M3BN cycle of isomerization and must be discharged together with 2M3BN, since the vapor pressures of 2M3BN and VCH are so close to one another that a separation is not possible by ordinary distillation. The reflux ratio of column K5 is adjusted so that 10 ppm T3PN are contained in stream 4. The draw-off amount of stream 4 from the top of column K5 is adjusted so that a total of 20% Z2M2BN and VCH are contained in top draw stream 13 of distillation column K3.

In column K5, a stream 5 (39 kg / h) is obtained via the gaseous side draw, which, in addition to 3-pentenenitriles, essentially contains the 2M3BN which has not been converted in the isomerization and, after condensation, is liquidly returned to column K3 as described above.

Example 2:

Example 2 is illustrated using FIG. 4.

In Example 2, a catalyst system based on nickel (0) complexes with chelate phosphite 2 as ligand is used for the hydrocyanation of BD:

In a step (1), the following streams are fed into a system consisting of two reactors R1a and R1b, each with a volume of 12 l, each of which is equipped with a nozzle, pulse exchange tube, external pumping circuit and in a heat exchanger in the pumping circuit for dissipating the reaction energy and are tempered to 363 K:

(1) 6 kg / h of liquid, unstabilized hydrogen cyanide freed from water by distillation to give R1a,

(2) 6 kg / h of liquid, unstabilized hydrogen cyanide freed from water by distillation to give R1 b,

(3) 25 kg / h BD to R1a, containing 0.25% C2BU, which was treated by contact with aluminum oxide to remove water and stabilizer TBC,

(4) 2 kg / h of recycled BD from column K2a in step (2) to R1a (stream 9), so that as a total BD feed to the reactor R1, a stream of 27 kg / h containing 98% BD and a total of 2% C2BU and 1-butene is obtained

(5) 14 kg / h of nickel (0) catalyst solution to R1a, obtained as described in this example below as stream 10a from column K2b

The stream 8 (54 kg / h) drawn off from the reactor R1 contains a total of 4% BD and C2BU, corresponding to a conversion of 94% BD, and a total of 74% pentenenitriles, of which 33% T3PN, 37% 2M3BN and small amounts of Z2M2BN and E2M2BN, among other pentenenitrile isomers as well as the catalyst components and catalyst degradation products and MGN.

Stream 8 is fed in a step (2) in a distillation column K2a, which is operated as a rectification column and is equipped with a falling film evaporator, and contains column internals with structured packing which generate 4 theoretical plates. Column K2a is operated at the head with a direct condenser which consists of a column section with a packed bed with total collecting cup, pump circuit and external heat exchanger. The column K2a is operated at an absolute top pressure of 0.8 bar, 263 K top temperature and 393 K bottom draw temperature.

Stream 9 is obtained at the top of column K2a and, as described at the beginning, is metered into the reactor R1a as a recycle stream. The reflux ratio at the top of column K2a is set so that the stream contains 90.1% 2M3BN. 52 kg / h of a stream 1 b which contains 0.3% BD, 0.1% C2BU, 76% pentenenitriles and additionally the catalyst constituents are obtained via the bottom of column K2a.

Stream 1b is moved in step (2) into a distillation column K2b, which is operated in the stripping mode and is equipped with falling film evaporator, top condenser with post-condenser and column internals with structured packing, which generate 4 theoretical plates. The column is operated at an absolute top pressure of 70 mbar, 333 K top temperature and 373 K bottom draw temperature.

At column K2b, the gaseous top draw stream 11 is obtained (40 kg / h), containing 0.4% BD, 54% 2M3BN and 42% T3PN and to a lesser extent E2M2BN and Z2M2BN along with other pentenenitrile isomers.

3 kg / h of a catalyst stream comprising a total of 45% pentenenitriles, 1.5% Ni (0) and the chelate ligand are fed into the column K2b, obtained, for example, by reacting nickel (0) (cyclooctadienyl) ₂ complex with the chelate phosphite 2. At the column K2b, the catalyst stream 10 containing 1.2% Ni (0), 0.3% 2M3BN and 17% residual pentenenitriles is obtained at the bottom. Stream 10 is partially returned to reactor R1 (14 kg / h) (stream 10a). Another part (stream 10b) (3.8 kg / h) is fed to a regeneration according to DE A-10351 002 to be used in the hydrocyanation of 3-pentenenitrile according to DE-A-102 004004683 or optionally in the hydrocyanation of BD to be recycled according to the inventive method.

The stream 11 is moved in a step (3) to a distillation column K3, which is equipped with a circulation evaporator and overhead condenser and with a structured packing which produce 45 theoretical plates. The column K3 is operated at an absolute top pressure of 1.0 bar, 395 K top temperature and 416 K bottom draw temperature.

24 kg / h of recycle stream 5 from column K5 in step (5), containing 70% T3PN, 14% 2M3BN and 7% Z2M2BN as well as small amounts of further pentenenitrile isomers, are fed into column K3.

Over the top of column K3, 30 kg / h of a stream 13 are obtained, containing 1% T3PN, 85% 2M3BN, 8% Z2M2BN and in total 3% BD and C2BU in addition to other pentenenitrile isomers and VCH. The reflux ratio of column K3 is adjusted so that 1% T3PN are obtained overhead. Over the bottom of column K3, 38 kg / h of stream 12 are obtained, containing a total of 97% T3PN, C3PN and 4PN and about 10 ppm 2M3BN and about 2% E2M2BN and in small amounts MGN and other pentenenitrile isomers.

In example 2, the chelate phosphite-based nickel (0) complex is used as the catalyst for the isomerization, as described for the hydrocyanation of BD in this example.

The stream 13 is fed in a step (4) together with a catalyst recycle stream 3a and a catalyst supplementary stream into a reactor R2, designed as a compartmentalized reactor with a tube characteristic and equipped with a preheater with which the reaction mixture is heated to 383 K. The sum of the recirculation catalyst and the fresh catalyst is fed into the reactor R2 12 kg / h of a mixture with 20% T3PN, 3% 2M3BN and other pentenenitrile isomers, 71% ligand mixture and 0.6% nickel (O) and a low content of catalyst degradation products ,

43 kg / h of stream 1 are obtained as product from reactor R2, containing 53% T3PN, 12% 2M3BN, corresponding to a conversion of 80% 2M3BN.

Stream 1 is passed in a step (5) into a distillation column K5, which is equipped with falling film evaporator, top condenser, reflux divider, gaseous side draw in the bottom region of the column and column internals which generate 30 theoretical plates. The column is operated at an absolute top pressure of 377 mbar, 355 K top temperature and 368 K bottom draw temperature.

The recovered catalyst stream 3 (11 kg / h) is obtained in column K5, comprising 20% T3PN in addition to other pentenenitriles, about 1% MGN and 0.6% Ni (0) and 54% ligand. A small part (stream 3b) is discharged to limit the leveling up of catalyst deactivation components and MGN. To supplement the discharged amount of catalyst, so much fresh catalyst containing 40% pentenenitrile isomers, 1.2% Ni (0) and 55% ligand mixture is metered in so that the Ni (0) content in the catalyst feed to the reactor R2 is kept at 0.6% ,

In column K5, a stream 4 is obtained overhead (1.4 kg / h), comprising a total of 18% BD and C2BU, 45% 2M3BN, 28% Z2M2BN, and small amounts of vinylcyclohexene (VCH). The reflux ratio of column K5 is adjusted so that 10 ppm T3PN are contained in stream 4. The draw-off amount of stream 4 from the top of column K8 is adjusted so that a total of 10% Z2M2BN and VCH are contained in top draw stream 13 of distillation column K3. In column K5, a stream 5 (24 kg / h) is obtained via the gaseous side draw, which in addition to 3-pentenenitriles essentially contains the 2M3BN not converted in the isomerization and, after condensation, is liquidly returned to column K3 as described above.

Example 3:

Example 3 is illustrated using FIG. 5.

In Example 3, a catalyst system based on nickel (0) complexes with a mixture of ligands is used for the hydrocyanation of butadiene. The ligand mixture for hydrocyanation contains approx. 60 mol% tri (m / p-tolyl) phosphite and 40 mol% chelate phosphate 2.

In a step (1), the following streams are fed into a system consisting of two reactors R1a and R1b, each with a volume of 12 l, each of which is equipped with a nozzle, pulse exchange tube, external pumping circuit and in a heat exchanger in the pumping circuit for dissipating the reaction energy and on 363 K are:

(1) 6 kg / h of liquid, unstabilized hydrogen cyanide freed from water by distillation to give R1 a,

(2) 6 kg / h of liquid, unstabilized, cyanohydrogen freed from water by distillation to give R1 b,

(3) 25 kg / h of commercial BD to R1a, containing 0.25% C2BU, which has been treated by contact with aluminum oxide to remove water and stabilizer TBC,

(4) 2 kg / h of recycled BD from column K2a in step (2) to R1a (stream 9), so that as a total BD feed to the reactor R1, a stream of 27 kg / h containing 98% BD and a total of 2% C2BU and 1-butene is obtained, (5) 14 kg / h of nickel (0) catalyst solution to R1a, obtained as stream 10a from column K2b as described in this example below

The stream 8 (54 kg / h) drawn off from the reactor R1 b contains a total of 4% BD and C2BU, corresponding to a conversion of 94% BD, and a total of 74% pentonitriles, of which 33% are T3PN, 37% 2M3BN and small amounts of Z2M2BN and E2M2BN, other pentenenitrile isomers, as well as the catalyst components and catalyst degradation products and MGN. Stream 8 is fed in a step (2) into a distillation column K2a, which is operated as a rectification column and is equipped with a falling film evaporator, and also contains column internals with structured packing which produce 4 theoretical plates. Column K2a is operated at the head with a direct condenser which consists of a column section equipped with a packed bed with total collecting cup, pump circuit and external heat exchanger. The column K2a is operated at an absolute top pressure of 0.8 bar, 263 K top temperature and 393 K bottom draw temperature.

Stream 9 is obtained at the top of column K2a and, as described at the beginning, is metered into the reactor R1a as a recycle stream. The reflux ratio at the top of column K2a is set so that the stream contains 90.1% 2M3BN.

52 kg / h of a stream 1b which contains 0.3% BD, 0.1% C2BU, 76% pentenenitriles and additionally the catalyst constituents are obtained at the bottom of column K2a.

5 kg / h of a catalyst stream are fed into the column K2b and, as described in Example 1 according to DE-A-102 004 004683, is obtained as a bottom draw from the column K4 from step (4) of Example 2, comprising a total of 45% pentenenitriles , 1.1% Ni (0), 38% ligand mixture and approx. 12% ADN.

The catalyst stream 10 comprising 1.2% Ni (0), 0.3% 2M3BN and 17% remaining pentenenitriles is obtained at the bottom of column K2b. Stream 10 is partially returned to reactor R1 (14 kg / h) (stream 10a). Another part (stream 10b) (3.8 kg / h) is fed to a regeneration according to DE-A-10351 002 in order to be used in the hydrocyanation of 3-pentenenitrile according to DE-A-102 004004683. The stream 11 is moved in a step (3) to a distillation column K3, which is equipped with a circulation evaporator and overhead condenser and with a structured packing which produce 45 theoretical plates. The column K3 is operated at an absolute top pressure of 1.0 bar, 395 K top temperature and 416 K bottom draw temperature.

28 kg / h of recycle stream 5 from column K6 in step (6), containing 72% T3PN, 15% 2M3BN and 8% Z2M2BN as well as small amounts of further pentenenitrile isomers, are fed into column K3.

Over the top of column K3, 30 kg / h of a stream 13 are obtained, containing 1% T3PN, 85% 2M3BN, 8% Z2M2BN and in total 3% BD and C2BU and other pentenenitrile isomers. The reflux ratio of column K3 is adjusted so that 1% 3PN are obtained overhead.

Over the bottom of column K3, 38 kg / h of stream 12 are obtained, containing a total of 97% T3PN, C3PN and 4PN and about 10 ppm 2M3BN and about 2% E2M2BN and in small amounts MGN and other pentenenitrile isomers.

In Example 3, a catalyst system based on nickel (0) complexes with a mixture of ligands is used for the isomerization of 2M3BN to T3PN. The ligand mixture for isomerization (hereinafter referred to as isomerization ligand) contains mixed phosphite ligands of the class P (OR) (OR ') (OR ") with statistically distributed R, R', R" from the group phenyl, m-tolyl, p-tolyl , o-tolyl, where more than 80 mol% of the sum of the residues R, R ', R "are m-tolyl and p-tolyl residues. Such ligand mixtures are used in the reaction of a mixture of m- and p-cresol (with a mixing ratio of 2: 1) from m- to p-cresol with a phosphorus trihalide Zinc chloride is used as a promoter for the isomerization reaction as described in US 3,676,481, US 3,852,329 and US 4,298,546.

The stream 13 is fed in a step (4) together with a catalyst recycle stream 3a and a catalyst supplementary stream into a reactor R2, designed as a compartmentalized reactor with a tube characteristic and equipped with a preheater with which the reaction mixture is heated to 383 K. The sum of the recirculation catalyst and fresh catalyst is fed into the R2 reactor 12 kg / h of a mixture with 20% T3PN, 3% 2M3BN and other pentenenitrile isomers, 71% isomerization ligand and 0.6% nickel (O) and a low content of catalyst degradation products.

43 kg / h of stream 1 are obtained as product from reactor R2, containing 53% T3PN, 12% 2M3BN, corresponding to a conversion of 80% 2M3BN. Stream 1 is moved in a step (5) into an evaporator stage B5, which is equipped with a forced-circulation evaporator and overhead condenser. The evaporator stage B5 is operated at an absolute pressure of 510 mbar, 403 K bottom draw temperature and 366 K condensation temperature.

In the evaporator stage B5, the recovered catalyst stream 3 (11 kg / h) is obtained, containing 20% T3PN in addition to other pentenenitriles, about 10% MGN and 0.5% Ni (0) and 61% ligand mixture. A small portion (stream 3b) is removed to limit the level of catalyst deactivation components and MGN. To supplement the discharged amount of catalyst, as much fresh catalyst is added, containing approx. 15% pentenenitrile isomers, approx. 2.0% Ni (0), approx. 70% isomerization ligand and the promoter zinc chloride in a concentration which corresponds to a molar ratio of ZnCl ₂ to nickel (O) of approx. 5 corresponds to the fact that the Ni (0) content in the catalyst feed to the reactor R2 is kept at 0.6%.

In the evaporator stage B5, stream 2 is obtained at the top condenser (25 kg / h), containing 1% BD, 68% T3PN, 16% 2M3BN and other pentenenitriles and small amounts of VCH.

Stream 2 is fed in a step (6) into the distillation column K6, which is operated as a rectification column and is equipped with a circulation evaporator, top condenser and column internals which generate 30 theoretical plates. The column is operated at an absolute top pressure of 340 mbar, 357 K top temperature, 313 K in the condenser and 373 K bottom draw temperature.

At the condenser of the column K6, about 100 standard l / h of a stream which essentially consists of BD is obtained as the gas phase.

In column K6, a stream 4 is obtained at the top condenser as the liquid phase (1.1 kg / h), comprising a total of 5% BD and C2BU, 50% 2M3BN, 30% Z2M2BN, and small amounts of vinylcyclohexene (VCH). The reflux ratio of column K6 is set so that 1 ppm of T3PN are contained in stream 4. The withdrawal amount of stream 4 from the top of column K6 is adjusted so that a total of 10% Z2M2BN and VCH are contained in the feed to reactor R2.

A stream 5 (24 kg / h) is obtained in column K6 (24 kg / h) which, in addition to 3-pentenenitriles, essentially contains 2M3BN which has not been converted in the isomerization and is returned to column K3 as described above.

Example 4:

Example 4 is illustrated with reference to FIG. 6. In Example 3, a catalyst system based on nickel (0) complexes with a mixture of ligands is used for the hydrocyanation of butadiene. The ligand mixture for hydrocyanation contains approximately 80 mol% of tri (m / p-tolyl) phosphite and 20 mol% of the chelate phosphite 2 (see Example 2).

In a step (1), the following streams are fed into a system consisting of three continuously operated stirred tanks R1a, R1b and R1c, each with a volume of 10 l, which are tempered to 373 K:

(1) 5.2 kg / h of liquid, unstabilized hydrogen cyanide freed from water by distillation to give R1 a,

(2) 4.0 kg / h of liquid, unstabilized, hydrogenated cyanide to R1 b,

(3) 20 kg / h 1 BD as stream 9 from the condenser of the evaporator B1 in step (2), containing 92% BD, 2% T3PN, 4% 2M3BN and approx. 2% C2BU to Ria, (4) 4.1 kg / h of nickel (0) catalyst solution to R1a, obtained as described in this example below as stream 3a from the evaporator stage B5 in step (5),

(5) 3.7 kg / h of nickel (0) catalyst solution for R1a, obtained as described in Example 3 according to the German patent application entitled "Process for the Production of Dinitriles" from BASF AG (B03 / 0525) as the bottom draw of the column K4 from step (4) of Example 2 is obtained, containing a total of 45% pentenenitriles, 1.1% Ni (0), 38% ligand mixture and about 12% ADN.

The reactor R1c is operated as a post-reactor with the outlet from reactor R1b at 353 K.

The stream 8 (37 kg / h) drawn off from the reactor R1c contains 1% BD, corresponding to a conversion of 98% BD, and in total 82% pentenenitriles, of which 36% T3PN, 44% 2M3BN and small amounts of Z2M2BN and E2M2BN, as well the catalyst components and catalyst degradation products and MGN and other pentenenitrile isomers.

Stream 8 is fed in a step (2) in an evaporator stage B1, which is equipped with a circulation evaporator. The evaporator stage B1 is equipped with a

Condenser operated, the condensed material from the return tank is rinsed. The evaporator stage B1 is operated at an absolute head pressure of 0.6 bar, 253 K condensation temperature and 363 K bottom draw temperature.

19.5 kg / h of commercial BD, containing 0.25% C2BU, which has been treated by contact with molecular sieve, are metered into the condensate collection container of evaporator stage B1, the water content of the BD used being removed to less than 10 ppm by weight of water ,

Stream 9 as the sum of the recycled and freshly metered in butadiene is withdrawn from the condensate collection container of the evaporator stage B1 and is returned to the reactor R1a as previously described.

37 kg / h of a stream 11b which contains 1% BD, 82% pentenenitriles and additionally the catalyst constituents are obtained via the bottom of the evaporator stage B1.

In a step (4), stream 11b is fed into a reactor R2 which is at a temperature of 383K and is designed as a stirred tank with a downstream residence time, 2M3BN being isomerized to T3PN in the presence of the nickel catalyst.

A pentenenitrile recycle stream 5 (10 kg / h), which is obtained in step (6) in column 6 as the bottom product, containing 60% 2M3BN, in total 10% T3PN with further pentenenitrile isomers and VCH and in small amounts, is fed into reactor R2 Quantities of BD.

A stream 1 is obtained from reactor R2 (45 kg / h), comprising 62% T3PN and 14% 2M3BN, corresponding to a conversion of 70% 2M3BN to T3PN, and the catalyst components.

Stream 1 is moved in a step (5) into an evaporator stage B5, which is equipped with falling film evaporator and condenser and is operated at an absolute pressure of 50 mbar and 393 K bottom draw temperature.

A stream 2 (38 kg / h) is obtained from the condenser of the evaporator stage B5, containing 91% pentenenitrile isomers and about 1% BD and to a lesser extent E2M2BN, Z2M2BN and VCH.

At the evaporator stage B5, the catalyst stream 3 is obtained at the bottom (7.2 kg / h), containing 1.2% Ni (0), 0.1% 2M3BN and 15% residual pentenenitriles. Stream 3 is partially (stream 3a) returned to reactor R1 (4.1 kg / h). The rest (stream 3b) is fed to a regeneration according to DE-A-103 51 002, and after the regeneration can be used, for example, in a hydrocyanation of 3-pentenenitrile as in Example 2 according to DE-A-102 004 004683 or can be used again as a catalyst in the process according to the invention for the hydrocyanation of butadiene, if appropriate after removal of zinc chloride.

The stream 2 is moved in a step (3) to a distillation column K3 which is equipped with a forced-circulation evaporator and overhead condenser and with column internals which generate 30 theoretical plates. The column K3 is operated at an absolute top pressure of 120 mbar, 334 K top temperature and 352 K bottom draw temperature.

10 kg / h of a stream 13 containing 5% T3PN, 60% 2M3BN, 4% Z2M2BN and in total 4% BD and C2BU and in the rest predominantly VCH are obtained at the top of column K3. The reflux ratio of column K3 is adjusted so that 5% T3PN are obtained overhead.

Over the bottom of column K3, 27 kg / h of stream 12 are obtained, containing a total of 98% T3PN, C3PN and 4PN and about 1000 ppm 2M3BN and about 2% E2M2BN.

In a step (6), stream 13 is fed into a distillation column K6, which is operated as a rectification column and is equipped with a forced-circulation evaporator, top condenser, reflux divider and column internals with structured packing, which generate 15 theoretical plates. The column K6 is operated at an absolute top pressure of 380 mbar, 361 K top temperature and 365 K bottom draw temperature.

In column K6, a liquid stream 4 is obtained overhead (0.6 kg / h), comprising a total of 4% BD and C2BU, 54% 2M3BN, 38% Z2M2BN, and 2.5% vinylcyclohexene (VCH). The draw-off amount of stream 4 from the top of column K6 is set such that a total of 30% Z2M2BN and VCH are present at top draw stream 13 of column K3. In column K6, a gaseous stream (195 standard l / h) is obtained on the top condenser, which is operated as a partial condenser, and essentially contains BD.

In column K6, stream 5 is obtained at the bottom (9.4 kg / h), which, in addition to 3-pentenenitriles, essentially contains the 2M3BN not converted in the isomerization and is returned to the isomerization reactor R2.

Example 5:

Example 5 is illustrated with reference to FIG. 7. In example 5, a catalyst system based on nickel (0) complexes with a mixture of ligands is used for the hydrocyanation of BD. The ligand mixture for hydrocyanation contains approximately 80 mol% of tri (m / p-tolyl) phosphite and 20 mol% of the chelate phosphonite 1 (see Example 1).

In a step (1), the following streams are fed into a system comprising two continuously operated stirred tanks R1a and R1b, each with a volume of 50 l and which are heated to 363 K: (1) 18 kg / h of liquid, unstabilized, by distillation water-freed hydrogen cyanide in equal parts to the reactors R1a and R1b,

(2) 62 kg / h BD as stream 9 from the top of the evaporator B1 in step (2), containing 87% BD, 3% T3PN, 6% 2M3BN and approx. 2% C2BU to reactor R1a, (3) 61 kg / h nickel (0) catalyst solution, obtained as described in this example below as stream 3a from evaporator stage B5 in step (5) to reactor R1a, (4) 6.7 kg / h nickel (0) catalyst solution to R1a, obtained as described in Example 1 according to the German patent application with the title “Process for the Production of Dinitriles” from BASF AG (B03 / 0525) 1 as a bottom draw from column K4 from step (4) of Example 2, comprising 45% in total Pentenenitrile, 1.1% Ni (0), 38% ligand mixture and approx. 12% ADN to reactor R1a, the butadiene stream and the catalyst stream being premixed before contacting with hydrogen cyanide.

Stream 8 (177 kg / h) withdrawn from reactor R1b contains 11% BD, corresponding to a conversion of 66% BD, and a total of 64% pentenenitriles, of which 32% T3PN, 30% 2M3BN and small amounts of Z2M2BN and E2M2BN and further pentenenitrile isomers, as well as the catalyst components and catalyst degradation products.

Stream 8 is fed in a step (2) in an evaporator stage B1, which is equipped with a falling film evaporator. The evaporator stage B1 is operated at the head with a condenser which is flushed with condensed material from the return tank. The evaporator stage B1 is operated at an absolute head pressure of 1.3 bar, 278 K condensation temperature and 403 K bottom draw temperature.

37 kg / h of commercial BD, containing 0.25% C2BU, which has been treated by contact with molecular sieve, are metered into the condensate collection container of evaporator stage B1, the water content of the BD used being less than 5 ppm by weight of water was removed and the stabilizer TBC contained in the BD used reaches concentrations in the ppm scale in the condensate collector and the condenser rinsing circuit.

Stream 9 is withdrawn as a sum of the recycled and freshly metered BD from the condensate collection container of the evaporator stage B1 and is returned to the reactor R1a as previously described.

152 kg / h of a stream 11b which contains 0.9% BD, 16% 2M3BN, 51% T3PN and further pentenenitrile isomers and additionally the catalyst constituents are obtained via the bottom of the evaporator stage B1. The composition of the bottom discharge of the evaporator stage suggests a degree of conversion of 50% 2M3BN to T3PN in the bottom of the evaporator B1.

Stream 11b is moved in a step (5) into an evaporator stage B5, which is equipped with falling film evaporator and condenser and is operated at an absolute pressure of 260 mbar and 383 K bottom draw temperature.

A stream 2 is obtained in gaseous form from the evaporator stage B5 (83 kg / h), comprising 93% pentenenitrile isomers and about 1% BD and to a lesser extent E2M2BN, Z2M2BN and VCH. Stream 2 is fed into the distillation column K3 in step (3).

At the evaporator stage B5, the catalyst stream 3 is obtained at the bottom (69 kg / h), containing 0.6% Ni (0), 2% 2M3BN and 42% remaining pentenenitriles. The majority of stream 3 is returned to the reactor R1 (61.4 kg / h) (stream 3a). The rest (stream 3b) is fed to a regeneration according to DE-A-103 51 002 and can be used, for example, in the hydrocyanation of 3-pentenenitrile, as described in Example 1 according to DE-A-102 004004 683.

In a step (3), stream 2 is passed in gaseous form to a distillation column K3 which is equipped with a forced air expansion evaporator and overhead condenser and with a structured packing which generate 30 theoretical plates. The column K3 is operated at an absolute top pressure of 80 mbar, 375 K top temperature and 343 K bottom draw temperature.

36 kg / h of a stream 13 containing 15% T3PN, 64% 2M3BN, 3% Z2M2BN and in total 4% BD and C2BU are obtained at the top of column K3, the rest predominantly containing VCH. The reflux ratio of column K3 is adjusted so that 15% T3PN are obtained overhead.

Over the bottom of column K3, 47 kg / h of stream 12 are obtained, containing a total of 98% T3PN, C3PN and 4PN as well as 100 ppm 2M3BN and approx. 1% E2M2BN. Stream 13 is passed in a step (6) into a distillation column K6, which is operated as a rectification column and is equipped with a forced circulation evaporator, top condenser, reflux divider and column internals with structured packing, which produce 45 theoretical plates. The column is operated at an absolute top pressure of 320 mbar, 288 K condensation temperature and 363 K bottom draw temperature.

In column K6, a liquid stream 4 is obtained overhead (6.8 kg / h), comprising a total of 10% BD and C2BU, 80% 2M3BN, 8% Z2M2BN, and 0.5% vinylcyclohexene (VCH). The draw-off amount of stream 4 from the top of column K6 is set such that a total of 15% Z2M2BN and VCH are present at top draw stream 3 of column K3. In column K6, a gaseous stream (263 standard l / h) is obtained at the top condenser, which is operated as a partial condenser, and essentially contains BD.

In column K6, stream 5 is obtained at the bottom (28.7 kg / h), which, in addition to 3-pentenenitriles, essentially contains the 2M3BN which has not been converted in the isomerization and is returned to the hydrocyanation reactor R1.

Example 6:

Example 6 is illustrated with reference to FIG. 8.

In example 8, a catalyst system based on nickel (0) complexes with chelate phosphonite 1 as ligand is used for the hydrocyanation of BD (see example 1).

In a step (1), the following streams are fed into a continuously operated stirred tank R1 of 30 1 volume, which is heated to 363 K: (1) 16 kg / h of liquid, unstabilized, hydrogen cyanide freed from distillation,

(2) 55 kg / h BD as stream 9 from the top of the evaporator B1 in step (2), containing 87% BD, 3% T3PN, 6% 2M3BN and approx. 2% C2BU,

(3) 10 kg / h of nickel (0) catalyst solution, obtained as described in this example below as stream 3a from evaporator stage B5 in step (5), comprising a total of 42% pentenenitriles, 23% ligand, 0.9% Nickel (O), as well as approx. 10% ADN and MGN,

(4) 4 kg / h of nickel (0) catalyst solution to R1, containing a total of 45% pentenenitriles, 1.5% Ni (0) and 48% ligand. The stream 8 (89 kg / h) drawn off from the reactor R1 contains 17% BD, corresponding to a conversion of 71% BD, and a total of 73% pentenenitriles, of which 32% T3PN, 36% 2M3BN and small amounts of Z2M2BN and E2M2BN, as well the catalyst components and catalyst degradation products.

34 kg / h of commercial BD, containing 0.25% C2BU, which has been treated by contact with aluminum oxide, are metered into the condensate collection container of the evaporator stage B1, the water content of the BD used being less than 10 ppm by weight of water and the TBC Content less than 10 ppm was reduced.

Stream 9 as the sum of the recycled and freshly metered in butadiene is withdrawn from the condensate collection container of the evaporator stage and returned to the reactor R1a, as previously described.

76 kg / h of a stream 5 which contains 0.8% BD, 12% 2M3BN, 69% T3PN and further pentenenitrile isomers and additionally the catalyst constituents are obtained via the bottom of the evaporator stage B1. The composition of the bottom discharge of the evaporator stage corresponds to a degree of conversion of 75% 2M3BN to T3PN in the bottom of the evaporator stage B1.

Stream 5 is moved in a step (5) into an evaporator stage B5, which is equipped with falling film evaporator and condenser and is operated at an absolute pressure of 220 mbar and 381 K bottom draw temperature.

A stream 2 is obtained in gaseous form from the evaporator stage B5 (58 kg / h), containing 97% pentenenitrile isomers and about 1% BD and to a lesser extent E2M2BN, Z2M2BN and VCH.

At the evaporator stage B5, the catalyst stream 3 is obtained at the bottom (17 kg / h), comprising 0.9% Ni (0), 0.3% 2M3BN and 42% residual pentenenitriles. The majority of stream 3 is returned to reactor R1 (10 kg / h) (stream 3a). The rest (stream 3b) is fed to a regeneration according to US 2003/0100442 and can be used after the regeneration in a hydrocyanation of 3-pentenenitrile or can be returned to the process for the hydrocyanation of BD in the process according to the invention. The stream 2 is condensed and liquid in a step (3) to a distillation column K3, which is equipped with a forced-circulation evaporator and overhead condenser and with a structured packing which generate 50 theoretical plates. The column K3 is operated at an absolute top pressure of 200 mbar, 342 K top temperature and 366 K bottom draw temperature.

A stream 4 containing 10% BD, 18% Z2M2BN, 68% 2M3BN and further pentenenitrile isomers and VCH is obtained at the top of the columns K3. The reflux ratio of column K3 is set so that the top draw stream contains 18% Z2M2BN.

8 kg / h of a stream 13 containing 0.5% T3PN, 85% 2M3BN, 5% Z2M2BN, 10% BD stream 13 are returned to the evaporator stage B1 on a liquid side draw off the column K3.

Over the bottom of column K3, 47 kg / h of stream 12 are obtained, containing a total of 98% T3PN, C3PN and 4PN as well as 100 ppm 2M3BN and approx. 1% E2M2BN.

All subsequent tests were carried out in a protective gas atmosphere.

Nickel (0) - [o-isopropylphenyl ₀ . ₈ -m- / p-tolyl ₃ . ₂ -phosphite] ₁₈ , (short: isopropyl catalyst); corresponds to a solution of 1.0% by weight of nickel (O) with 19% by weight of 3PN and 80% by weight of o-isopropylphenyl ₀ .sm- / p-tolyl ₃ . ₂ -phosphite.

Examples for the continuous hydrocyanation of BD to 2M3BN / 3PN

Example 7 (comparison): (ratio BD / HCN = 1.4: 1)

2.11 mol of moist and stabilized butadiene (100 ppm water, 100 ppm TBC), 1.55 mol HCN and 14 mmol Ni in the form of the isopropyl catalyst are fed into a pressure reactor per hour (pressure: 15 bar, temperature inside 105 ° C, Residence time: approx. 40 min / reactor). The HCN turnover is quantitative according to dimensional analysis (Vollhard titration). The ratio 2M3BN / 3PN of the reaction discharge is determined by GC chromatography (GC area percent). The ratio 2M3BN / 3PN was 1.95 / 1. The loss of Ni (0) based on the value product formed was: 0.58 kg Ni (0) / t value product (3PN / 2M3BN).

Example 8: (ratio BD / HCN = 1.4: 1) 2.13 mol of butadiene dried over a bed of 4 Å molecular sieve, 1.53 mol of HCN and 14 mmol of Ni in the form of the isopropyl catalyst are fed into a pressure reactor per hour (pressure: 15 bar, temperature inside 105 ° C., residence time: approx. 40 min / reactor). The HCN turnover is quantitative according to dimensional analysis (Vollhard titration). The ratio 2M3BN / 3PN of the reaction discharge is determined by GC chromatography (GC area percent). The ratio 2M3BN / 3PN was 1.95 / 1. The loss of Ni (0) based on the value product formed was: 0.14 kg Ni (0) / t value product (3PN / 2M3BN).

Example 9: (ratio BD / HCN = 1.2: 1)

2.09 mol of butadiene dried over a bed of aluminum oxide, 1.67 mol of HCN and 14 mmol of Ni in the form of the isopropyl catalyst are fed into a pressure reactor per hour (pressure: 15 bar, temperature inside 105 ° C., residence time: approx. 45 min /Reactor). The HCN turnover is quantitative according to dimensional analysis (Vollhard titration). The ratio 2M3BN / 3PN of the reaction discharge is determined by GC chromatography (GC area percent). The ratio 2M3BN / 3PN was 1.95 / 1. The loss of Ni (0) based on the product of value formed was: <0.10 kg Ni (0) / t product of value (3PN / 2M3BN).

Examples of the continuous isomerization of 2M3BN to 3PN

Example 10:

A hydrocyanation discharge prepared according to Example 8 is collected and excess BD is removed by distillation. The mixture thus obtained is heated to 130 ° C for one hour. After 0, 30 min and after 1 h, GC samples are taken from the reaction mixture and examined by GC chromatography (GC area percent).

Examples of incorrect isomerization of 2M3BN to 2M2BN by recycled hydrocyanation catalyst

Example 11: 100 g of isopropyl catalyst are continuously withdrawn from a catalyst reservoir filled with 649 g of fresh isopropyl catalyst at t = 0 h and, together with 2.14 mol of butadiene dried over a bed of aluminum oxide, and 1.67 mol of HCN per hour are fed into a pressure reactor (Pressure: 15 bar, temperature inside 105 ° C, residence time: approx. 45 min / reactor). The HCN turnover is quantitative according to dimensional analysis (Vollhard titration). The product of value is continuously separated from the catalyst by means of a Sambay distillation and the back catalyst thus obtained is returned to the reservoir. The reaction is operated for 50 h and the still hydrocyanation-active catalyst is discharged due to the beginning of the secondary component 2M2BN. The catalyst obtained in this way is subjected to isomerization tests:

Example 12 (comparison):

10 g of isomerization catalyst are spiked with 2M3BN (15 g) and annealed at 120 ° C. for 5 h. With a conversion of 89% 2M3BN (GC area percent), 8.6% incorrect isomers (2M2BN) are found.

Example 13:

N-Heptane (100 g) and adiponitrile (50 g) are added to the isomerization catalyst from Example 11 (100 g) and the mixture is stirred (15 min). After phase separation (30 min) the lower phase is drained. Part of the upper phase (50 g, heptane + isomerization catalyst) is concentrated on a rotary evaporator. The residue (14 g, isomerization catalyst) is topped up with 2M3BN (21 g) and heated at 120 ° C. for 5 h. With a conversion of 95% 2M3BN (GC area percent), 2.0% incorrect isomers (2M2BN) are found.

Example 14:

The residues of the upper phase from the first extraction (Example 12) are again mixed with adiponitrile (37.5 g) and stirred. After phase separation, part of the upper phase is again concentrated on a rotary evaporator and the residue (9.3 g) is increased with 2M3BN (14 g). After 5 h at 120 ° C., a 2M3BN conversion of 94% (GC area percent) and a faulty isomerization of 0.7% are evident. Examples of incorrect isomerization of 2M3BN to 2M2BN using a continuously used isomerization catalyst

Example 15:

300 g of isopropyl catalyst are introduced into a 21 reactor and 450 g / h of 2M3BN are added continuously and the mixture is heated to 130.degree. With a residence time of 60 minutes, the reactor contents are continuously removed and worked up by distillation, and the isomerization catalyst remaining in the bottom is recycled. The reaction is operated for 50 h and the isomerization-active catalyst is discharged due to the beginning of isomerization of 2M3BN. The catalyst obtained in this way is subjected to isomerization tests:

Example 16:

10 g of isomerization catalyst are spiked with 2M3BN (15 g) and annealed at 120 ° C. for 5 h. With a conversion of 90% 2M3BN (GC area percent), 9.8% incorrect isomers (2M2BN) were found.

Example 17:

N-Heptane (100 g) and adiponitrile (50 g) are added to the isomerization catalyst from Example 16 (100 g) and the mixture is stirred (15 min). After phase separation (30 min) the lower phase is drained. Part of the upper phase (50 g, heptane + isomerization catalyst) is concentrated on a rotary evaporator. The residue (14 g, isomerization catalyst) is topped up with 2M3BN (21 g) and heated at 120 ° C. for 5 h. With a conversion of 93% 2M3BN (GC area percent), 2.4% incorrect isomers (2M2BN) were found.

Example 18:

The residues of the upper phase from the first extraction (Example 17) are again mixed with adiponitrile (37.5 g) and stirred. After phase separation, part of the upper phase is again concentrated on a rotary evaporator and the residue (9.3 g) is replenished with 2M3BN (14 g). After 5 h at 120 ° C, a 2M3BN conversion of 93% (GC area percent) and a faulty isomerization of 0.6% are evident.

Claims

claims

1. Process for the preparation of 3-pentenenitrile, characterized by the following process steps:

(a) isomerization of a reactant stream which contains 2-methyl-3-butenenitrile over at least one dissolved or dispersed isomerization catalyst to a stream 1 which comprises the at least one isomerization catalyst, 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z) Contains -2-methyl-2-butenenitrile,

(b) Distillation of stream 1 to give a stream 2 as top product which contains 2-methyl-3-butenenitrile, 3-pentenenitrile and (Z) -2-methyl-2-butenenitrile, and a stream 3 as bottom product which is the contains at least one isomerization catalyst,

2. The method according to claim 1, characterized in that the educt stream is obtained by the following process steps: (e) hydrocyanation of 1,3-butadiene over at least one hydrocyanation catalyst with hydrogen cyanide to give a stream 8 which comprises the at least one hydrocyanation catalyst, 3-pentenenitrile , 2-methyl-3-butenenitrile, 1, 3-butadiene and residues of hydrogen cyanide, (f) one or more distillation of stream 8 to obtain a stream 9 which contains 1, 3-butadiene, a stream 10 which the contains at least one hydrocyanation catalyst, and a stream 11 which contains 3-pentenenitrile and 2-methyl-3-butenenitrile, (g) distillation of stream 11 to give a stream 12 as bottom product which contains 3-pentenenitrile and a stream 13 as Top product containing 2-methyl-3-butenenitrile.

3. The method according to claim 2, characterized in that process steps (d) and (g) are carried out in the same distillation device, streams 6 and 12 and streams 7 and 13 coinciding.

4. The method according to any one of claims 2 or 3, characterized in that process steps (c) and (g) are carried out in a common distillation column, process step (d) being omitted, stream 2 from process step (b) and stream 11 from Process step (f) are carried out in process step (g), in process step (g) the stream 4 as top product containing (Z) -2-methyl-2-butenenitrile, the stream 12 as bottom product containing 3-pentenenitrile and the stream 13 can be obtained as a side draw stream containing 2-methyl-3-butenenitrile.

5. The method according to any one of claims 1 to 4, characterized in that the at least one isomerization catalyst obtained in process step (b) in stream 3 is recycled to process step (a).

6. The method according to any one of claims 1 to 5, characterized in that process steps (b) and (c) are carried out together in a distillation device, stream 3, which contains the at least one isomerization catalyst, as bottom product, stream 4, the (Z) contains -2-methyl-2-butenenitrile as top product and stream 5, which contains 3-pentenenitrile and 2-methyl-3-butenenitriI, is obtained on a side draw of the column.

7. The method according to any one of claims 1 to 5, characterized in that the process steps (a), (b) and (c) are carried out together in a distillation device, the stream 4, the (Z) -2-methyl-2 -butenenitrile contains, as top product, stream 5, which contains 3-pentenenitrile and 2-methyl-3-butenenitrile, are obtained at a side draw of the distillation apparatus and the isomerization catalyst remains in the bottom of the distillation column.

8. The method according to any one of claims 1 to 7, characterized in that the isomerization catalyst nickel (O), a nickel (O) as a ligand complexing, containing trivalent phosphorus compound and optionally a Lewis acid.

9. The method according to any one of claims 1 to 8, characterized in that the pressure and temperature in process step (b) are set so that the isomerization catalyst is less active than in process step (a) or is not active.

10. The method according to any one of claims 1 to 8, characterized in that the hydrocyanation catalyst and the isomerization catalyst are identical.

11. The method according to any one of claims 1 to 10, characterized in that the educt stream is obtained by the following process steps:

(a *) Isomerization of a starting material stream which contains 2-methyl-3-butenenitrile over at least one dissolved or dispersed isomerization catalyst to a stream 1 which contains the at least one isomerization catalyst, 2-methyl-3-butenenitrile, 3-pentenenitrile and Contains (Z) -2-methyl-2-butenenitrile,

(b *) Distillation of stream 1 to give a stream 2 as overhead product which contains 2-methyl-3-butenenitrile, 3-pentene nitrile and (Z) -2-methyl-2-butenenitrile, and a stream 3 as Bottom product which contains the at least one isomerization catalyst,

(c *) distillation of stream 2 to give a stream 4 as overhead product which is enriched with respect to stream 2 in (Z) -2-methyl-2-butenenitrile, based on the sum of all pentenenitriles in stream 2, and a stream 5 as bottom product which is enriched with respect to stream 2 in 3-pentenenitrile and 2-methyl-3-butenenitrile, based on the sum of all pentenenitriles in stream 2,

(d *) Distillation of stream 5 to obtain stream 6 as bottom product which contains 3-pentenenitrile and stream 7 as top product which contains 2-methyl-3-butenenitrile. (h *) catalyst regeneration to increase the nickel (0) content of the partial streams 14 from stream 3 or 16 from stream 10 to produce a stream 18,

Extraction of stream 18, if necessary stream 19, with respect to the catalyst components and / or interfering component (s) by adding a di-nitrile stream 20 and a hydrocarbon stream 21 to produce two immiscible phases 22 and 23, stream 22 being the predominant part of the catalyst components and stream 23 contains the major part of the interference component, (k *) separation of the hydrocarbon from the catalyst components from stream 22 by distillation to produce a stream 25 which contains the majority of the catalyst components and, if appropriate, partial or complete recycling of the stream 25 to process steps (a *) or (e * )

(e *) Hydrocyanation of 1,3-butadiene over at least one hydrocyanation catalyst using hydrogen cyanide to obtain a stream 8 which contains the at least one hydrocyanation catalyst, 3-pentenenitrile, 2-methyl-3-butenenitrile, 1,3-butadiene and residues of hydrogen cyanide .

(f *) single or multiple distillation of stream 8 to obtain stream 9 which contains 1,3-butadiene, stream 10 which contains at least one hydrocyanation catalyst and stream 11 which comprises 3-pentenenitrile and 2 Contains methyl-3-butenenitriI,

(g *) Distillation of stream 11 to obtain a stream 12 as the bottom product which contains 3-pentenenitrile and a stream 13 as the top product which contains 2-methyl-3-butenenitrile.

12. The method according to claim 11, characterized in that in step h *) the increase in the nickel (0) catalyst content is carried out by reductive catalyst regeneration.

13. The method according to any one of claims 11 or 12, characterized in that the catalyst guide is operated as two separate catalyst circuits, one circuit having stages e *) and f *) and the other circuit having stages a *), b *) and c *).

14. The method according to any one of claims 11 to 13, characterized in that stabilizer-containing butadiene is used as feed stream to e *).

15. The method according to any one of claims 11 to 14, characterized in that phosphites of the formula I b

P (OR ¹ ) _x (OR ² ) _y (OR ³ ) _z (OR ⁴ ) _p (I b) with

R ¹ : aromatic radical with a C ¹ -C ₈ -alkyl substituent in the o-position to the oxygen atom which connects the phosphorus atom with the aromatic system binds, or with an aromatic substituent in the o-position to the oxygen atom that connects the phosphorus atom to the aromatic system, or with an aromatic system fused in the o-position to the oxygen atom that connects the phosphorus atom to the aromatic system,

R ² : aromatic radical with a CC ₁₈ alkyl substituent in the m position to the oxygen atom which connects the phosphorus atom to the aromatic system, or with an aromatic substituent in the m position to the oxygen atom which connects the phosphorus atom to the aromatic system, or with an aromatic system fused in the m-position to the oxygen atom which connects the phosphorus atom to the aromatic system, the aromatic residue in the o-position to the oxygen atom which connects the phosphorus atom to the aromatic system carries a hydrogen atom .

R ³ : aromatic residue with a d-cis-alkyl substituent in the p-position to the oxygen atom that connects the phosphorus atom to the aromatic system, or with an aromatic substituent in the p-position to the oxygen atom that connects the phosphorus atom with the aromatic system , where the aromatic radical in the o-position to the oxygen atom that connects the phosphorus atom to the aromatic system carries a hydrogen atom, R ⁴ : aromatic radical in the o-, m- and p-position to the oxygen atom that the phosphorus atom connects to the aromatic system, carries substituents other than those defined for R ¹ , R ² and R ³ , the aromatic radical in the o-position to the oxygen atom which connects the phosphorus atom to the aromatic system carries a hydrogen atom, x: 1 or 2, y, z, p: independently of one another 0, 1 or 2 with the proviso that x + y + z + p = 3.

16. The method according to any one of claims 11 to 15, characterized in that the catalysts are phosphites of the formula I b P (OR ¹ ) _x (OR ² ) _y (OR ³ ) _z (OR ⁴ ) _p (I b) wherein R ¹ , R ² and R ^{3 are} independently selected from o-isopropyl phenyl, m-tolyl and p-tolyl, R ^{4 is} phenyl; x is 1 or 2 and y, z, p are independently 0, 1 or 2 with the proviso that x + y + z + p = 3; and mixtures thereof, ie mixtures of 2 or more, preferably 2 to 10, particularly preferably 2 to 6, of the compounds of the formula Ib.